CN207584765U

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

Info

Publication number: CN207584765U
Application number: CN201590000837.4U
Authority: CN
Inventors: 雷约·利利坎坷斯
Original assignee: Ollon Technology Co Ltd
Current assignee: Ollon Technology Co Ltd
Priority date: 2015-03-03
Filing date: 2015-12-03
Publication date: 2018-07-06
Anticipated expiration: 2025-12-03
Also published as: WO2016139387A1; WO2016139385A1

Abstract

The utility model is related to be used to generate the catalysis combustion plant and 3 stage catalytic combustion plants of energy with high efficiency.The catalysis combustion plant (CAB) is including at least with lower component：Primary air supply source (AIR1), for at least the 90% of burning air needed for (CAB) will to be catalyzed, it is delivered to as primary air (AIR1) in the preceding part (CAS) of the catalysis combustion plant (CAB)；At least two successive fuel supply sources (FU1, FU2, FU3, FU4), for supplying fuel in the catalysis combustion plant (CAB)；With at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4)；At least one heat transfer component (HT1, HT2, HT3)；The exhaust apparatus (EXH) of the gas (EXG) for discharge burning generation in the tail portion (CAL) of the catalysis combustion plant (CAB).

Description

It burns for generating the catalysis combustion plant of energy and 3 stage catalytics with high efficiency Facility

Technical field

The method that the utility model is related to be used to generate energy with high efficiency and extremely low discharge.The utility model further relates to fit Together in the manufacture and use of the equipment of this method and the equipment.

Background technology

The whole world nitrogen oxides, carbon monoxide, carbon dioxide and hydrocarbon caused by all in bound energy production Discharge, for inhibit greenhouse effects.It has been that heat boiler, technique equipment, smelting furnace etc. propose for the purpose in Europe Several instructions.These instructions include the discharge standard for greenhouse gases limited directly or indirectly through efficiency.In the U.S., EPA (Bureau for Environmental Protection) and especially CARB (adding state Air Resources Board) are had been carried out for nitrogen oxides and nytron The stringent regulation of object (some are with compound particular form).CO2 emission is supervised by the efficiency of boiler and smelting furnace It surveys.China is undergoing similar development.It is had been set in Beijing, such as the limits value of the nitrogen oxides from boiler 30mg/m³, and 80mg/m is had been set to for the limits value of CO gas³.These be not further processed In the case of, with the current irrealizable standard stringent in this way of the hot combustion plant of tradition.In other industrialization fields of China Continue to the identical trend tightened energetically.

Global climate forum is seeking the growth in order to prevent greenhouse gases and is realizing the complete of stable falling tendency The scheme of ball agreement.Most difficult purpose is to inhibit fossil fuel particularly burning of coal.The carbon dioxide formed in burning Largely along with nitrogen oxide, when temperature rise is to 1100 DEG C or more the accumulation of nitrogen oxide rapidly accelerate, imitating In the case that rate does not decline, this can not be to avoid in the heat burning of gas and liquid.U.S.'s pot of operation in the U.S. Stove Manufacturers Association (ABMA) has about 800 member company.It is relatively low output boiler (<Manufacturer 115kW) it is not qualified into For its member.Based on this, approx the estimation whole world there are the company of this size of 4000-5000 family's manufacture is 4000- to height 5000, and the quantity of the boiler therefore manufactured is about 500.000 pcs/.

Instead of the post processing of flue gas, ultralow NO_x(UltraLow NO_x) and without NO_x(Zero NO_x) burner business Manufacturer uses the preheating of flue gas recirculation, water emulsification and gas in its burner mixed energetically.Although referred to as nothing NO_x, but neither one heat burning manufacturer has reached zero NO_xDischarge.The value of minimum report is all under 3% oxygen level 6ppm (about 12mg/m³)。

Second option is the cleaning of flue gas.The removal of nitrogen oxides usually by using selective catalytic converter or Non-selective catalytic converter (SCR, NSCR) carries out.Therefore the highest clean rate obtained at a temperature of about 300 DEG C is about 98%.However, SCR catalytic converter requires individual reducing agent, urea or ammonia, this by incur in fuel costs about 4% volume Outer cost.Whereby available NO_xEmission level is about 5-20ppm.In addition, CO discharge standards are frequently necessary to individually aoxidize Catalyst.

As a kind of new product, market has existed for 3 effects that are common, being suitable in boiler in a kind of automobile and is catalyzed Converter, but the adjustment of air/fuel ratio will be subjected to the stringent regulation of 3 effect catalysts.This technology even more so that Current quite stringent NO can be obtained_xWith CO limits values.

As summary above, it is inferred that the clean method of heat burning and flue gas associated with it cannot generate reality Without discharge (NO on border_x, VOC and CO) thermal energy, and the thermal energy can use the catalytic combustion device and cleaning of the utility model Fuel generates.Therefore, even if uniquely harmful discharge (that is, carbon dioxide (CO2)) can be used in applying for such as plant In fertilizer, as protective gas, industrial raw materials etc..

Plant is for nitrogen oxide (NO_x), sulfur oxide (SO_x), hydrogen sulfide (H2S) and ethylene (C2H4) it is quick Sense is about 100 times (referring to following table) of people.In the case of the catalysed oxidation processes of the utility model, it might even be possible to realize plant It is required that emission level.Subsequent table shows that people is for most heavy in the work environment compared with the acceptable concentration of plant The acceptable concentration (male, 8h working days) for endangering gas wanted.

Carbon dioxide fertilization is the most useful in vegetable cultivation.There are about 1000 temperature in the present vegetable cultivation of Finland Room, and in these greenhouses about 330 fertilising is performed by using the liquid or gaseous carbon dioxide of about 5,000,000 kg/ of total amount. Price Range is extensive：In maximum consignment (consignment), liquid CO₂About 0,10 euro/kg are spent, and it is bottled CO₂Spend about 1,5 euro/kg.Compared with the consumption of Finland, the consumption of estimating the whole world is Finland's consumption more than 200 times.In greenhouse In use, CO₂Market be about 300,000,000 euro/year, but if not being the liquid CO that small greenhouse uses₂It is that such expensive market may It is so great that more.

Fuel does not allow to include any compound being harmful to catalyst, such as organic precious metal and silicon compound, Do not allow to include halogenated hydrocarbons yet.Similarly, the amount of particle must be limited (it is recommended that less than 1mg/Nm³)。

Utility model content

Now apllied is a kind of method for being used to generate energy with high efficiency and extremely low discharge.The utility model also relates to And a kind of manufacture of equipment and the equipment for being suitable for this method and use (purposes).

It is according to the present utility model in a first aspect, a kind of catalysis combustion plant for being used to generate energy with high efficiency, special Sign is that the catalysis combustion plant is included at least with lower component：

Primary air supply source for that will be catalyzed at least 90% of air needed for burning, is delivered as primary air Into the preceding part of the catalysis combustion plant；

- at least two successive fuel supply sources, for supplying fuel in the catalysis combustion plant；At least two A successive catalysis combustion phases, it is primary in the preceding part of the catalysis combustion plant by being delivered in each stage Air, in the time frame of 0.015-0.10s, only gradually catalytically combustion order supply fuel so that it is described catalysis combustion Temperature in the burning stage 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 described excessive empty Gas be based on remnant oxygen and be measured, and it is described be catalyzed combustion phases in fuel/air rate under lower explosion limit, and And

Wherein, the catalyst for the catalysis combustion phases is mixed catalytic converter, and the mixed catalytic turns Parallel operation includes the noble metal from metal beehive；

At least one heat transfer component, for reducing the gas generated at least one successive catalysis combustion phases Temperature, and the heat transfer component is before next successive catalysis combustion phases；

The exhaust apparatus of the gas for discharge burning generation in the tail portion of the catalysis combustion plant.

Further, the tail portion of the catalysis combustion plant is provided at least one remaining heat transfer component, is used for The temperature of the gas of the burning generation is reduced in the downstream of the catalysis combustion phases.

Further, the heat transfer component and/or the remaining heat transfer component have tube designs.

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

Further, the catalysis combustion plant is provided at least one static mixing before the catalysis combustion phases Device.

Further, the catalysis combustion plant is provided with secondary air supply source, and the secondary air supply source is used for Air is delivered, and the air that the secondary air supply source is delivered is not more than 10% of air needed for catalysis burning.

Further, there are heat exchangers between the catalyst.

Further, the downstream of the catalyst is provided with temperature sensor.

Further, the primary air supply source is used to be catalyzed at least 99% conduct of air needed for burning Primary air is delivered in the preceding part of the catalysis combustion plant.

Further, in each stage in described at least two successive catalysis combustion phases, by being delivered to The primary air in the preceding part of catalysis combustion plant is stated, in the time frame of 0.02-0.06s, is only gradually catalytically burnt suitable The fuel of sequence supply so that the temperature in the catalysis combustion phases is higher than 800 DEG C and less than 1000 DEG C.

Further, the heat transfer component and/or the remaining heat transfer component are designed with finned tube.

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

On the other hand, a kind of 3 stage catalytic combustion plants, which is characterized in that the 3 stage catalytic combustion plant is included extremely Less with lower component：

Primary fuel supply source for that will be catalyzed at least 90% of fuel needed for burning, is supplied to 3 rank In the preceding part of Duan Cuihua combustion plants；

For 3 successive oxygen supply sources that oxygen is supplied in the 3 stage catalytic combustion plant；And it uses It gradually burns 3 of the fuel successive only catalysis combustion phases in the oxygen by delivering；

- two successive heat transfer components, for reducing the gas generated in three successive catalysis combustion phases Temperature, and the heat transfer component is before next successive catalysis combustion phases；

Being filled for discharging the exhaust of the gas of burning generation in the tail portion of the 3 stage catalytic combustion plant It puts,

Wherein, the catalyst for the catalysis combustion phases is mixed catalytic converter, and the mixed catalytic turns Parallel operation includes the noble metal from metal beehive.

Further, the tail portion setting of the 3 stage catalytic combustion plant is used for there are one remaining heat transfer component The temperature of the gas of the burning generation is reduced after the catalysis combustion phases.

Further, the 3 stage catalytic combustion plant further includes the condenser of the gas for generation of burning.

Further, the catalyst for the catalysis combustion phases is provided with heat exchanger, and the heat is handed over Parallel operation has the diagonal corrugated plating stacked in the vertical direction so that the wave crest of ripple intersects in different directions, to establish Intersection in the shape of alphabetical X extends circulation road, thus establishes hybrid cellular structure.

Further, the hybrid cellular structure of the catalyst is soldered to be attached with shell in its end.

Further, the primary fuel supply source will be supplied at least 99% of fuel needed for catalysis burning In the preceding part of the 3 stage catalytic combustion plant.

On the other hand, the fuel/air rate in combustion phases CA1, CA2, CA3, CA4 is catalyzed is in LEL (lower explosion limit) Under.The first method of the utility model includes at least following steps：

Primary air will be used as at least 90% of air needed for catalysis burning (CAB), preferably at least 99% (AIR1) it is delivered in the preceding part of catalysis combustion plant (CAB)；

Fuel (FU1, FU2, FU3, FU4) is supplied to catalysis combustion plant (CAB) at least two successive phases In, and pass through delivering in each stage at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4) To catalysis combustion plant (CAB) preceding part (CAS) in primary air (AIR1), 0,015-0,10s time frame (when Between range, time frame) in, preferably in the range of 0,02-0,06s, only gradually catalytically combustion order supply combustion Expect (FU1, FU2, FU3, FU4) so that the temperature in catalysis combustion phases (CA1, CA2, CA3, CA4) is higher than 800 DEG C and low In 1100 DEG C, 1000 DEG C are preferably lower than, wherein, catalysis burning is that the excess air measured to remnant oxygen carries out, and And the fuel/air rate in catalysis combustion phases (CA1, CA2, CA3, CA4) is under LEL (lower explosion limit)；

It is reduced at least one hot transfer stages (HT1, HT2, HT3) at least one successive catalysis combustion phases The temperature of the gas (EXG) generated in (CA1, CA2, CA3, CA4), the hot transfer stages (HT1, HT2, HT3) are next It is catalyzed before combustion phases (CA1, CA2, CA3, CA4)；

The gas (EXG) of burning generation is removed from the tail portion (CAL) of combustion plant (CAB).

This solution provides simple technology application, and technique becomes efficient, and the discharge of result will be extremely low.

Remnant oxygen means the amount (w/w) of the oxygen in the gas of the after-combustion generation of catalysis burning in this application.

Second aspect according to the present utility model, the fuel/air mixture in combustion phases CA1, CA2, CA3, CA4 is catalyzed Than on UEL (upper explosion limit).The second method of the utility model includes at least following steps：

At least the 90% of fuel (FUE) will be catalyzed in burning (CAB), preferably at least 99% is delivered to catalysis burning In the preceding part of facility (CAB)；

Oxidizing gas or liquid (OXY) are supplied at least two successive phases in catalysis combustion plant (CAB), And in each stage, in the time frame of 0,015-0,10s, preferably in the time frame of 0,02-0,06s, only gradually urge Change supply fuel (FUE) of the ground burning at least two in succession catalysis combustion phases (CA1, CA2, CA3, CA4), so that Temperature in catalysis combustion phases (CA1, CA2, CA3, CA4) is preferably lower than 1000 higher than 800 DEG C and less than 1100 DEG C DEG C, and wherein, fuel/air rate in catalysis combustion phases (CA1, CA2, CA3, CA4) UEL (upper explosion limit) it On；

Temperature is sufficiently high for efficiency combustor fuel at this time.Temperature is so low so that not generating simultaneously NO_xDischarge.Temperature is also beneficial to component (assembling).

One side according to the present utility model, the utility model include to be catalyzed air needed for burning CAB not More than 10%, preferably no more than 1% is delivered to as auxiliary air AIR2 under the preceding part CAS of catalysis combustion plant CAB Trip.One side according to the present utility model, the utility model include that at least 99% of air needed for burning CAB will be catalyzed It is delivered to as primary air AIR1 in the preceding part CAS of catalysis combustion plant CAB.This is provided for burning and/or its efficiency It is further to strengthen.

In burning according to the present utility model, including only catalytically burning, it will bring no NOx emission or NOx dense Degree is extremely low.Therefore it does not need to remove NOx from discharge gas.The discharge of carbon monoxide (CO) and hydrocarbon (CH) To be extremely low.Compared with prior art processes, the advantages of this provides technology and economic two aspect with high efficiency and extremely low discharge.

One side according to the present utility model, the utility model are included fuel FU1, FU2, FU3, FU4 at least three It is supplied in a successive phases in catalysis combustion plant CAB, and the preceding part CAS by being delivered to catalysis combustion plant CAB In primary air AIR1, at least three successive catalysis combustion phases CA1, CA2, CA3, CA4 gradually combustion order supply Fuel FU1, FU2, FU3, the FU4 given.Correspondingly, the utility model be included at least two hot transfer stages HT1, HT2, The temperature of gas EXG generated at least two in succession catalysis combustion phases CA1, CA2, CA3, CA4 is reduced in HT3, it is described Hot transfer stages HT1, HT2, HT3 are before next successive catalysis combustion phases CA1, CA2, CA3, CA4.This provides burning And/or its efficiency further enhances.

One side according to the present utility model, the utility model are included fuel FU1, FU2, FU3, FU4 at least four It is supplied in a successive phases in catalysis combustion plant CAB, and the preceding part CAS by being delivered to catalysis combustion plant CAB In primary air AIR1, at least four successive catalysis combustion phases CA1, CA2, CA3, CA4 gradually combustion order supply Fuel FU1, FU2, FU3, the FU4 given.Correspondingly, the utility model be included at least three hot transfer stages HT1, HT2, The temperature of gas EXG generated at least two successive catalysis combustion phases CA1, CA2, CA3, CA4, institute are reduced in HT3 Hot transfer stages HT1, HT2, HT3 are stated before next successive catalysis combustion phases CA1, CA2, CA3, CA4.This provides combustion It burns and/or its efficiency further enhances.

One side according to the present utility model, the utility model includes will be in air needed for catalysis burning CAB At least 99% is delivered to as primary air AIR1 in the preceding part CAS of catalysis combustion plant CAB.According to the present utility model one A aspect, the utility model include being not more than 10% as auxiliary air AIR2 using in air needed for catalysis burning CAB It is delivered to the downstream of the preceding part CAS of catalysis combustion plant CAB.This provides burning and/or its efficiency further enhances.

One side according to the present utility model, the utility model are included in catalysis combustion phases CA1, CA2, CA3, CA4 The gas of burning generation is reduced in the tail portion CAL of the combustion plant CAB in downstream at least one residual heat transfer stages HT4 The temperature of body EXG.One side according to the present utility model, the utility model are included in hot transfer stages HT1, HT2, HT3 And/or the gas EXG by generation of burning in residual heat transfer stages HT4 is cooled to 150-350 DEG C of temperature.According to this practicality Novel one side, the utility model are included at least one hot transfer stages HT1, HT2, HT3 and/or in residual heat The thermal energy that includes in the gas EXG of recycling burning generation in transfer stages HT4, and transfer thermal energy to water, air or other In liquid or gaseous material.One side according to the present utility model, the utility model include the gas EXG generated that will burn And/or CO₂In the thermal energy that includes directly preferably utilized in the greenhouse in the position used.This provides burning and/or its effect Rate further enhances.

One side according to the present utility model, fuel FU1, FU2, FU3, the FU4 supplied are gaseous state and/or liquid 's.One side according to the present utility model, fuel FU1, FU2, FU3, the FU4 supplied, which is selected from, includes natural gas, biology Air-liquid gas, light fuel oil, alcohols, carbon monoxide, the substance generated in the heat treatment of timber group.It can also be other Fuel gas and liquid.This provides burning and/or its efficiency further enhances.Preferably pass through air in several stages It is aoxidized.Oxygen and other oxidation liquid or gaseous material can also be used.

One side according to the present utility model, the temperature being catalyzed in combustion phases CA1, CA2, CA3, CA4 are less than 1100 DEG C, preferably less than 1000 DEG C, even more preferably less than 900 DEG C.One side according to the present utility model, catalysis burning rank Burning in section CA1, CA2, CA3, CA4 carries out in the time frame of 0,015-0,10s.This provides burning and/or its efficiency Further enhance.

One side according to the present utility model, when being converted into thermal energy calculating with the energy that fuel includes, catalysis burning Gross efficiency be at least 99%.This provides burning and/or its efficiency further enhances.

One side according to the present utility model, the nitrogen oxides NO from the discharge gas EG of catalysis burning discharge_x's Concentration is averaged less than 1ppm.One side according to the present utility model, the oxygen from the discharge gas EG of catalysis burning discharge Change the concentration of carbon CO averaged less than 1ppm.One side according to the present utility model, from the discharge gas EG of catalysis burning discharge In volatile hydrocarbon VOC concentration averaged less than 1ppm.This provides burning and/or the further increasing of its efficiency By force.

One side according to the present utility model, the first and/or second fuel supply FU1 and burn relative to catalysis is supplied to The percentage of the total amount of fuel FU1, FU2, FU3, FU4 in facility CAB is determined on the basis of the calorific value of fuel, side Formula is that the temperature of the first catalyst will not be risen to more than 1000 DEG C, is more than 900 DEG C preferably without rising to.This It provides burning and/or its efficiency further enhances.

One side according to the present utility model, catalysis combustion phases CA1, CA2, CA3, CA4 by using comprising from The mixed catalytic converter of the noble metal of metallic monomer (cell) carries out.This provide burning and/or its efficiency it is further Enhancing.

One side according to the present utility model, the last one catalyst can be bigger than other catalysts, with Just ensure cleaning burning.According to fuel, preceding catalyst can have to be become in the range of 60.000-300.000 1/h The treating capacity (throughput) of change.In the last one catalyst, output can advantageously be 30.000- 200.000 1/h.This provides burning and/or its efficiency further enhances.

It can be manufactured according to the catalytic combustion device of the utility model first aspect by following steps：

At least one preceding part (CAS) is set for catalysis combustion plant (CAB), the forepart point includes at least one primary Air supply source (AIR1) is being catalyzed at least 90% of air needed for burning (CAB), preferably at least for delivering 99%；

In the downstream of preceding part (CAS), at least two successive fuel supply sources are set for catalysis combustion plant (CAB) (FU1, FU2, FU3, FU4), for supplying fuel in catalysis combustion plant (CAB)；

For catalysis combustion plant (CAB), at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4) are set, In each stage, by the primary air (AIR1) being delivered in the preceding part (CAS) of catalysis combustion plant (CAB), 0, In the time frame of 015-0,10s, preferably in the time frame of 0,02-0,06s, the only gradually catalytically combustion of combustion order supply Expect (FU1, FU2, FU3, FU4) so that temperature in catalysis combustion phases (CA1, CA2, CA3, CA4) more than 800 DEG C and Less than 1100 DEG C, preferably less than 1000 DEG C, wherein, catalysis burning is carried out by the excess air measured with remnant oxygen, and The fuel/air rate in combustion phases (CA1, CA2, CA3, CA4) is catalyzed under LEL (lower explosion limit)；

At least one heat transfer component (HT1, HT2, HT3) is set for catalysis combustion plant (CAB), for reducing extremely The temperature of gas (EXG) generated in a few successive catalysis combustion phases (CA1, CA2, CA3, CA4), and the heat passes Component (HT1, HT2, HT3) is passed before next successive catalysis combustion phases (CA1, CA2, CA3, CA4)；

Exhaust apparatus (EXH) is set for catalysis combustion plant (CAB), in the tail portion of combustion plant (CAB) (CAL) gas (EXG) of the burning generation in.

It can be manufactured according to the catalytic combustion device of the utility model second aspect by following steps：

At least one preceding part (CAS) is set for catalysis combustion plant (CAB), at least one forepart point is included at least One primary fuel supply source (FUE) is used for delivering and is being catalyzed at least 90% of fuel needed for burning (CAB), preferably Ground at least 99%；

It is that catalysis combustion plant (CAB) sets at least two successive oxidizing gas or liquid in the downstream of preceding part (CAS) Body supply source (OXY), for supplying fuel in catalysis combustion plant (CAB)；

For catalysis combustion plant (CAB), at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4) are set, In each stage, in the time frame of 0,015-0,10s, preferably in the time frame of 0,02-0,06s, only gradually it is catalyzed Ground burning fuel (FUE), so that the temperature in catalysis combustion phases (CA1, CA2, CA3, CA4) is more than 800 DEG C and few In 1100 DEG C, preferably less than 1000 DEG C, and wherein, fuel in catalysis combustion phases (CA1, CA2, CA3, CA4)/ Air ratio is on UEL (upper explosion limit)；

It is set in the tail portion (CAL) of combustion apparatus (CAB) for catalysis combustion plant (CAB) for discharge burning The exhaust apparatus (EXH) of the gas (EXG) of generation,.

One side according to the present utility model, catalysis combustion plant CAB are provided at least in its tail portion CAL One residual heat transfer stages HT4, for reducing the gas of burning generation after combustion phases CA1, CA2, CA3, CA4 is catalyzed The temperature of body EXG.One side according to the present utility model, heat transfer component HT1, HT2, HT3 and/residual heat transfer stages HT4 has tube designs.One side according to the present utility model, the supply of sequence fuel FU1, FU2, FU3, FU4 are suitably for gas State or liquid fuel.One side according to the present utility model, for being catalyzed the catalysis of combustion phases CA1, CA2, CA3, CA4 Converter is the mixed catalytic converter comprising the noble metal from metal beehive.One side according to the present utility model, The downstream of the preceding part CAS of combustion plant CAB is catalyzed, catalysis combustion plant CAB is provided with secondary air supply source AIR2, should Secondary air supply source can be used for delivering not more than 10% of air needed for catalysis burning CAB.

The catalysis combustion plant of first aspect according to the present utility model includes：

Primary air supply source (AIR1), at least the 90% of burning air needed for (CAB) will to be catalyzed, preferably Ground at least 99% is delivered to as primary air (AIR1) in the preceding part (CAS) of catalysis combustion plant (CAB)；

For supply fuel at least two successive fuel supply sources in catalysis combustion plant (CAB) (FU1, FU2, FU3, FU4) and at least two successive catalysis combustion phases (CA1, CA2, CA3, CA4), in each stage, pass through delivering It is excellent in the time frame of 0,015-0,10s to the primary air (AIR1) in the preceding part (CAS) of catalysis combustion plant (CAB) Selection of land in the time frame of 0,02-0,06s, only gradually catalytically combustion order supply fuel (FU1, FU2, FU3, FU4), So that the temperature in catalysis combustion phases (CA1, CA2, CA3, CA4) is more than 800 DEG C and less than 1100 DEG C, it is preferably few In 1000 DEG C, wherein, catalysis burning is carried out, and urging by the excess air measured with remnant oxygen (being preferably 1-3%) Change the fuel/air rate in combustion phases (CA1, CA2, CA3, CA4) under LEL (lower explosion limit)；

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 One is catalyzed before combustion phases (CA1, CA2, CA3, CA4) in succession；

It is filled in the tail portion (CAL) of combustion apparatus (CAB) for discharging the exhaust of the gas (EXG) of burning generation It puts (EXH).

Included according to the catalysis combustion plant of the utility model second aspect：

Primary fuel supply source (FUE), at least 90% of fuel needed for burning (CAB) will to be catalyzed, preferably Ground at least 99% is delivered to as primary (AIR1) in the preceding part (CAS) of catalysis combustion plant (CAB)；

It is used to providing oxidizing gas or liquid supply at least two oxidations in succession in catalysis combustion plant (CAB) Gas or liquid supply source (OXY) and at least two are catalyzed combustion phases (CA1, CA2, CA3, CA4) in succession, in each stage In, in the time frame of 0,015-0,10s, preferably in the time frame of 0,02-0,06s, only gradually catalytically combustion order The fuel (FU1, FU2, FU3, FU4) of supply, so that the temperature in catalysis combustion phases (CA1, CA2, CA3, CA4) is more In 800 DEG C and less than 1100 DEG C, preferably less than 1000 DEG C, and wherein, catalysis combustion phases (CA1, CA2, CA3, CA4 the fuel/air rate in) is on UEL (upper explosion limit)；

One side according to the present utility model, catalysis combustion plant CAB are provided at least one in its tail portion CAL A remnants heat transfer component HT4, for reducing the gas of burning generation after combustion phases CA1, CA2, CA3, CA4 is catalyzed The temperature of EXG.

One side according to the present utility model, heat transfer component HT1, HT2, HT3 and/or remaining heat transfer component HT4 With tube designs.

One side according to the present utility model, for being catalyzed the catalyst of combustion phases CA1, CA2, CA3, CA4 For the mixed catalytic converter comprising the noble metal from metal beehive.

One side according to the present utility model, in the downstream of the preceding part CAS of catalysis combustion plant CAB, catalysis burning Facility CAB is provided with secondary air supply source AIR2, which can be used for delivering institute in CAB is burnt in catalysis Need not more than the 10% of air.

One side according to the present utility model, the supply of sequence fuel FU1, FU2, FU3, FU4 are suitable for gaseous state or liquid is fired Material.

In this application, refer to be disappeared for used fuel completely burned in air needed for catalysis burning CAB The amount of the air of consumption.It further includes to ensure the possible excess air needed for completely burned.The excess air can conduct Primary air or auxiliary air are delivered.

The sequence in component and stage is reported with reference to the flow direction of primary air AIR1.

Unless in addition report, otherwise used average value is 24 hourly average values.

The catalysis process of the utility model can be more using dilute air fuel mixture that the mode of heat is difficult to burn It is aoxidized in a successive phases so that gas always cools down after the stage.Therefore, maximum temperature can be adjusted to so It is low, so that not generating NO_xDischarge.This method allows to realize generates energy, and be practically without nitrogen oxidation with high efficiency Object (NO_x), the discharge of VOC and carbon dioxide (CO).These temperature are in terms of oxidation of hydrocarbons and CO gas Be it is best, aoxidize so efficiently so that do not generate discharge (<1ppm).In addition to suboxides temperature, high speed catalysis oxidation excludes NO_xFormation, which is about 0,02-0,06 second, is aflame about 20 times of heat.Another contribution because Element is Fast Cooling immediately after oxidation.

The completely burned of fuel is promoted by the mixed metal honeycomb type catalyst comprising noble metal.Mixed structure carries Significantly increasing for mass transfer (that is, reactant being diffused into the hole of active coating) is supplied.It is activated with metal oxide basis Other catalysts such as ceramic honeycomb monomer be also useful, but these do not have above-mentioned catalyst effectively and Persistently.

Catalysis burning is that oxidation can perform the unique method to generate nitrogen oxides not at all by it, because It can be carried out in the case where specific heat burns significantly lower temperature and substantially higher rate.During oxidation of high density, Temperature also rises to very high level in catalyst or even specific heat is aflame much higher, because such as its name institute It represents, catalyst, which is catalyzed or accelerates, to be reacted and substantially increase temperature.It is if useful several in heat is burnt The admixture of gas of stoichiometry catalytically aoxidizes in the single stage, then according to modeling, temperature will rise to about 2500℃.Using the equipment of the utility model, it is difficult to by the way that several stages that are divided into will be aoxidized, and by oxidation with the side of heat Dilute mixture that formula is effectively burned, temperature can maintain the temperature less than 1000 DEG C.Being catalyzed an advantage of burning is Very high efficiency of combustion, even with dilute mixture.In fact, its efficiency of combustion is 100%.

Device according to the present utility model, which is characterized in that aoxidized in several stages, mode is so that is firing Air/oxygen in burning needed for all stages always exists in the reaction, and substance to be oxidized is added in a manner of substep Into air-flow.It is aoxidized in each stage with catalyst.Exothermic oxidation reaction is divided into several stages makes highest Temperature can drop to desired level.The cooling gas between oxidation stage.

In heat is burnt, there is the stringent limitation for lighting fuel/air mixture.About methane, for example, point burner There are about 5% lower limit (LEL) and about 15% upper limit (UEL).About 10% fuel/sky is usually used in burning in conventional boiler Gas mixture occurs, this is close to stoichiometric ratio.

In catalysis oxidation, limitation is than in hot aflame much more relaxed.In the case of no support energy, it is less than 1% mixture can be aoxidized.Similarly, the Methane/air more than 15% can be partly aoxidized simply by the presence of oxygen Mixture.Therefore, oxidation or the rising of temperature simultaneously can be adjusted with the concentration of fuel gas or oxygen.

If natural gas is aoxidized for example in three phases, then the amount of fuel will be mixture in each stage About 3,3%.In this case, the temperature in catalyst will remain in less than about 1000 DEG C.Each catalytic oxidation stage First cooling gas in a heat exchanger is followed by before next oxidation stage, is preferably cooled to about 150-350 DEG C.Cold But during, in heat transfer to water, air or some other media.

The utility model enables not only dilute air/fuel mixture partly to aoxidize, but also makes rich admixture of gas It can partly aoxidize, so as to some in only oxygenated fuel.Purpose can aoxidize desired part or desired ingredient, Such as by hydrogen from fuel complete oxidation, and carbon only partial oxidation is into the CO gas for being used as industrial raw materials. Partial oxidation can with oxidant, gradually make-up fuel stream performs by before each catalyst.

The feature of the utility model includes：

1. dilute mixture

Aoxidized with several successive catalysts, mode be so that oxidation needed for air amount almost All catalysts all or all are advanced through, but substance to be oxidized is individually injected into each catalytic conversion In device, temperature will not be increased over 1000 DEG C (Figure 1A to Fig. 5) for a long time in each catalyst.

Catalysis burning carries out to the excess air that remnant oxygen measures.One side according to the present utility model is being come The amount of remnant oxygen is 0.5-10% in the gas (EXG) of the burning generation of the tail portion (CAL) of spontaneous combustion facility (CAB), Preferably 1-3%.

There is preferably heat exchanger between catalyst, wherein, by liquid or gaseous medium by gas cooling To about 150-350 DEG C.Only substance to be oxidized before each catalyst where its oxidation is delivered, therefore again will Temperature increases to about 1000 DEG C (service chart 1A-1C) at its peak

Supplying it to be divided into two enables especially dilute fuel/air mixture by catalytically oxygen to four-stage Change.The principle can be used for constructing oxidation equipment, which does not generate nitrogen oxides (NO_x), and The discharge of carbon monoxide (CO) and hydrocarbon (CH) also by it is extremely low (<1ppm).The realization of the emission level significantly by X flowing catalysts (X-Flow catalytic converter) described in utility model NO.10627.

There is the ability that catalyst is used to aoxidize lean fuel mixture, the performance of boiler can individually use fuel Volume adjust or can be adjusted together with the volume of air.

Adoptable fuel include gaseous state or liquid cleaning fuel, such as natural gas and liquefied gas, low-sulfur light oil, alcohols, Biogas and biofluid etc..As long as fuel does not include nitrogen compound, nitrogen oxides would not be generated.

Flue gas can be in the unrefined CO for greenhouse₂Fertilising.Because it in this case, is included in Thermal energy in flue gas is also put into use, and the thermal efficiency of boiler rises to almost 100%.

Recuperative heat exchanger enables various gaseous states and liquid to be heated.In this case, facility is for example right The boilers such as space heating and useful hot water, steam, the warm air of industrial technology.

The principle shown in service chart 1A-1C can also be applied to construct air heater with recuperative heat exchanger Function.

Boiler allows concurrently to use the various energy, natural gas, fuel oil, alcohols etc..Primary air is supplied and two Secondary air supply can also include VOC compound or other burning cpds aoxidized in the catalyst.From these of supply The concentration maximum of gas can be the 20% of AEL.It controls the temperature sensor of fuel supply that can reduce fuel by control to supply It should.

- the first and it is most important application made by the catalyst activated with noble metal (such as platinum (Pt) and palladium (Pd)) Into.Metal oxide basis (such as oxide of lanthanum, cerium, nickel, copper, chromium, tungsten, manganese, iron, cobalt, barium) can also use.Above-mentioned Combination can also use, but these enliven not as noble metal or its mixed oxide and can be lasting.

2. rich mixture

In the case of the entire amount of not enough oxygen combustion fuel, facility can also be transported in rich mixture Row (>The UEL limit).In this case, lasting air-flow will be the air of the amount needed for sequence partial oxidation, purity oxygen Or the fuel that other oxidizing gas or liquid sequentially supplement.If it is necessary, can be delivered together with fuel cooling reaction or Promote the water of selective oxidation.

One side according to the present utility model, at least the 90% of fuel, preferably more than 99% is advanced through entire technique, And the air of controlled quatity is delivered before each catalyst.It therefore would be advantageous to pursue partial oxidation, mode Hydrogen to be for example only contained in gas is aoxidized by selective catalyst and the oxidation of carbon is restricted to carbon monoxide.Such as In the case that 900 DEG C of the hot gas including CO can be used in such as hardened steel.Technology application about this method and equipment can To be carried out as in above application, but the delivering of fuel and air is opposite as one sees fit.

One side according to the present utility model, catalysis combustion plant (CAB) by catalysis combustion phases (CA1, CA2, CA3, CA4) it is carried out before using at least one static mixer.This generates strong turbulence fluids.

Facility can be made of three identical heating modules and hot transfer module.Heating module (being preferably 2 to 4) Including fuel supply, vertically and horizontally static mixer and catalyst converter.After each heating module, exist can by series connection or Heat spreader (heat transfer) made of finned tube in parallel.Some modules are also used as the condensation to discharge gas Device recuperation of heat.

Description of the drawings

Several embodiments of the utility model are shown in Figure 1A to Fig. 7：

Figure 1A shows that 2 stages including primary air supply source and secondary air supply source and tubing heat exchanger urge Change combustion apparatus.

Figure 1B shows that 3 stages including primary air supply source and secondary air supply source and tubing heat exchanger urge Change combustion apparatus.

Fig. 1 C show that 4 stages including primary air supply source and secondary air supply source and tubing heat exchanger urge Change combustion apparatus.

Fig. 2 shows including primary air supply source and secondary air supply source and at external jacket (outer jacket) In lasting heat exchanger (continuous heat exchanger) 3 stage catalytic combustion apparatus.

Fig. 3 shows 3 sections of heat exchanges including primary air supply source and secondary air supply source and in external jacket 3 stage catalytic combustion apparatus of device.

Fig. 4 shows its heat and discharges the 3 stage catalytic combustion apparatus that gas is used in greenhouse.

Fig. 5 shows 3 stage catalytic combustion apparatus of fuel supply and the supply of 3 stage oxygen including 1 stage.

Fig. 6 shows the service chart of the combustion plant supplied with 3 stage fuels.

Fig. 7 shows the service chart of the combustion plant supplied with 3 stage oxygen.

Specific embodiment

Catalysis combustion plant as shown in Figure 1A-1C and Fig. 2-3 includes：Primary air supply source AIR1, for inciting somebody to action At least the 90% of air needed for catalysis burning CAB, preferably at least 99% is delivered to catalysis as primary air AIR1 fires In the preceding part CAS for burning facility CAB；For delivering fuel into 2-4 in catalysis combustion plant CAB fuel supply sources in succession FU1, FU2, FU3, FU4 and 2-4 successive only catalysis combustion phases CA1, CA2, CA3, CA4, are delivered to for passing through Be catalyzed combustion plant preceding part CAS in primary air AIR1 step by step combustion order supply fuel FU1, FU2, FU3, FU4；Include the heat transfer component HT of 1-3 heat transfer component HT1, HT2, HT3, urged for reducing at least one successive Change the temperature of gas EXG generated in combustion phases CA1, CA2, CA3, and described heat transfer component HT1, HT2, HT3 exist Before next successive catalysis combustion phases CA1, CA2, CA3, CA4；Exhaust apparatus EXH, in the tail of combustion plant CAB The gas EXG of burning generation in the CAL of portion part.The tail portion CAL for being catalyzed combustion plant CAB sets there are one residual heats to pass Component HT4 is passed, for reducing the temperature of the gas EXG of burning generation after combustion phases CA1, CA2, CA3, CA4 is catalyzed Degree.Cold water W_{It is cold}Combustion plant is had been conducted through, for generating hot water W_HeatAnd/or warm water W_Temperature。

According to Figure 1A-1C and Fig. 2-3, catalysis combustion plant further includes secondary air supply source AIR2.

According to Figure 1A -1C, heat transfer component HT1, HT2, HT3 and/or remaining heat transfer component HT4 have tube designs. According to fig. 2, heat transfer component HT1, HT2, HT3 is included in external jacket and by lasting structure composition, and the implementation of Fig. 3 Scheme is included in individual heat transfer component HT1, HT2, HT3 in external jacket.

Fig. 4 shows that gas EXG that is consistent with Fig. 2, making its burning generation and hot water utilize in greenhouse Green Catalytic combustion device.

Fig. 5 describes 3 stage catalytic combustion plants, including：Primary fuel supply source FUE, for that will be catalyzed in burning CAB At least the 90% of required fuel, preferably at least 99% is supplied in the preceding part CAS of catalysis combustion plant CAB；For inciting somebody to action Oxygen delivery to 3 successive oxygen in catalysis combustion plant supply OXY and 3 successive only catalysis combustion phases CA1, CA2, CA3, for passing through the oxygen of delivering gradually burning fuel FUE；There are two the heat of successive heat transfer component HT1, HT2 for tool Transferring element HT, for reducing the temperature of gas EXG generated in three in succession catalysis combustion phases CA1, CA2, CA3, and And described heat transfer component HT1, HT2, HT3 are before next successive catalysis combustion phases CA1, CA2, CA3；Exhaust apparatus EXH, for the gas EXG of the burning generation in the tail portion CAL of combustion plant CAB.It is catalyzed the tail of combustion plant CAB CAL settings in portion part are there are one remaining heat transfer component HT4, for after combustion phases CA1, CA2, CA3, CA4 is catalyzed Reduce the temperature of the gas EXG of burning generation.Cold water W is cold to have been conducted through combustion plant, for generating hot water W heat. The present embodiment further includes the condenser COOL for burning gases EXG, produces warm water W wherein_TemperatureAnd discharge gas and Condense EXC.

Production figure in Fig. 6 includes：Fuel FU1, FU2, FU3 are supplied to catalysis combustion plant in three successive phases It is successive at three in CAB, and the primary air AIR1 by being delivered in the preceding part CAS of catalysis combustion plant CAB Fuel FU1, FU2, FU3 that gradually combustion order supplies in only catalysis combustion phases CA1, CA2, CA3；In two hot transfer stages In HT1, HT2, the temperature of gas EXG generated at least one successive catalysis combustion phases CA1, CA2, CA3 is reduced, it is described Hot transfer stages HT1, HT2 are before next successive catalysis combustion phases CA1, CA2, CA3, CA4；From combustion plant CAB's Tail portion CAL removes the gas EXG of burning generation.There are one remaining for the tail portion CAL settings of catalysis combustion plant CAB Heat transfer component HT4, for reducing the temperature of the gas EXG of burning generation after combustion phases CA1, CA2, CA3 is catalyzed Degree.Cold water W_{It is cold}Combustion apparatus is had been conducted through, for generating hot water W_HeatAnd/or warm water W_Temperature.Catalysis combustion plant also wraps Include secondary air supply source AIR2.

Production figure in Fig. 7 includes：Primary fuel supply source FUE in the preceding part CAS of combustion apparatus CAB；For By oxygen delivery to 3 successive oxygen supply source OXY in catalysis combustion plant CAB and 3 be catalyzed in succession combustion phases CA1, CA2, CA3, for passing through the oxygen of delivery order gradually burning fuel FUE；Include the heat of 2 heat transfer components HT1, HT2 Transferring element HT, for reducing the temperature of gas EXG generated in three in succession catalysis combustion phases CA1, CA2, CA3, and And heat transfer component HT1, HT2 is before next successive catalysis combustion phases CA1, CA2, CA3；Exhaust apparatus EXH, For the gas EXG of the burning generation in the tail portion CAL of combustion apparatus CAB.It is catalyzed the tail portion portion of combustion plant CAB Divide CAL settings there are one remaining heat transfer component HT4, for being reduced after combustion phases CA1, CA2, CA3, CA4 is catalyzed The temperature of the gas EXG of burning generation.Cold water W_{It is cold}Combustion plant is had been conducted through, for generating hot water W_Heat。

In the equipment of the utility model, used heat exchanger can include various recuperative heat exchangers or regeneration Formula heat exchanger can be made of the stainless grade of steel of common boiler or such as 1.4512 and 1.4509.In catalyst In, it is preferred to employ the high temperature grade of steel of such as 1.4767 FeCrAl alloyings.

Cast recuperative heat exchanger will form the main body of boiler, especially when substance to be heated is liquid.It is real Two different principles can be based on by applying.According to convective principles, water passes through in pipe, and burning gases pass through to and fro outside pipe (Figure 1A -1C) several times.Preferably using the small pipe of diameter because in this way pipe then have it is big for area of section External surface area.Even if this is because heat transfer coefficient from gas to steel when its maximum compared with the coefficient from steel to water Also only it is its about 1/10th.

By setting pipe that can enhance hot transmission so that burning gases is enable to form turbulence stream in exchanger.Not only use Training wall mixing (flow guiding walls Mix) can further enhance hot transmission, and with the steel construction subregion detached Can also, the subregion from inside by forcefully making tube swelling, to generate the contact surface of the metal being close to and metal It is engaged with pipe.It is required that the subregion has the thickness (1,5-2mm) for the effective heat transfer abundance from gas to steel pipe.Finned tube As another useful option transmitted for heat of the enhancing from gas to metal.

It will be flowed with airtight subregion and be preferably divided into two to four sections, in each section, gas passes through a series of Pipe passes through once back and forth.Before each section, gas passes through catalyst.

Catalyst is heated to about 450-650 DEG C of temperature to swash by the facility by using injector (injector) Living, after this, flame can be off and catalyst starts oxidizing gas, and the supply of air and gas can simultaneously To rise to basic horizontal.

In general, it is somebody's turn to do with the equal fuel used with facility continuous operation but with the fuel and air stream activation of reduction Facility, and fuel/air mixture is in the highly combustible range close to stoichiometric mixture, the fuel/air mixture Mixture object is lighted with the standard ignitor used in the boiler.Each catalytic converter injects and lights unit Ign in fuel Later.Preferably delivered fuel into thermal current before catalyst, so as to for liquid fuel provide the time with It vaporizes and equably mixes before reaching catalyst.

Secondary adjustment can be carried out by reducing the supply of fuel in boiler performance, and main adjustment can lead to It crosses and cuts down the supply of both fuel and air to carry out.

The downstream of catalyst is provided with the temperature sensor that can be used for monitoring catalyst operation.If temperature Drop under setting lower limit (such as 700 DEG C), then activation pattern will be rebuild.

The last one catalyst can have the treating capacity lower than the catalyst of forefront (leading) (to handle up Amount), wherein, according to fuel, which can preferably change in the range of 60.000-300.000 1/h.Last In one, in order to realize that zero level discharges, treating capacity can be preferably in the range of 40.000-200.000 1/h.

The equipment can make its capacity (capacity) vary to height, such as 10kW-100MW from low.

Presented below is two embodiments of the boiler of described type, for its manufactured size calculate and model calculate with And schematic diagram 1A-1C and schematic diagram 3.

The designing scheme of structure and its key dimension and industrial grade specification of the embodiment 1 based on tubing heat exchanger is such as Shown in lower：

Fuel can be natural gas or such as (biology) ethyl alcohol.

It is 50MW with the boiler capacity of natural gas, and with bio-ethanol is then about 29MW.Same facility can be used for two Person, but fuel nozzle and the fuel quantity of injection of various stages must change, for reaching foot in the two of the beginning stage Enough high temperature (800-950 DEG C).The dosage of natural gas is preferably distributed by 36%, 32% and 32% successively.Point of ethyl alcohol With will be preferably 36%, 32% and 32%.Ensured completely with a small amount of excess airs that remnant oxygen (preferably 1-3%) measures Burning.

Catalyst type is as follows：

First catalyst and the second catalyst are 4000 × 1200 × 120mm (W × H × L), and have There are the volume of 576dm3, the treating capacity of 95.500 1/h, void density 100cpsi and load 70g/ft3Pd.

Other aspects of third catalyst are all identical, in addition to the length with 150mm, the volume of 720 dm3 And 76.400 1/h treating capacity.

The first catalyst is injected with entirely measure the 36% of fuel, so as to which gas temperature rises to about from+20 DEG C 850 DEG C, it is cooled to about 350 DEG C in a heat exchanger.

Second catalyst and third catalyst receive the 32% of fuel, so as to which temperature rise is to about 900 DEG C.

On the basis of flowing turbulence in heat exchanger is caused, calculated with heat transfer coefficient 180W/m2oK.

It manages as 40 × 8000mm of DIN, in total about 500 barred bodies (rod), material 1.4512.

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

The pressure loss is about 5000Pa.

In this case, conventional tubular heat exchanger has been utilized in the boiler described in Figure 1A -1C, wherein, such as scheme It is presented in 1A-1C, water (fluid) is advanced in the duct, and the gas heated is advanced through catalyst and tubular type to and fro Honeycomb.

The scale diagrams of second embodiment are shown in FIG. 3.Thermal capacity with this boiler of natural gas is about 1MW, and be 0,58MW with ethyl alcohol.

Boiler is assembled by three elements, which is provided with mixing X flow patterns catalyst and heat exchanger.As Extension can include similar element, and in the case of the catalyst not for increasing efficiency, element as such is Heat exchanger.

Heat exchanger has the diagonal corrugated plating (diagonally corrugated plate) stacked in vertical direction, So that the wave crest (crest) of ripple intersects in different directions, circulation is extended with the intersection established in the shape of letter X Road.Therefore the hybrid cellular shape structure established is by using such as resistance welding (capacitor discharge or seam welding (seam Welding)) or laser welding is welded in its end, to be attached with shell.Therefore the surface of the shell of construction has at it On the shell made of plate so that leave the gap of about 25mm between them, flow water to be heated in the gap.Multi-disc Steel plate is soldered Uniform Flow and heat transmission to enhance water.

Each element includes the inlet and outlet pipe for hot fluid to be added.Pipeline is usually connected in series with, mode For cold water is caused to flow to front end from the aft end of boiler.Pipeline can also be connected in parallel, therefore provided three individual water and added Hot loop.

The boiler of Fig. 3 can be assembled by the element with flange connections (flange joint).Outer surface equipped with every Heat.This modular structure top of each other and can also be formed by being mounted on element by circulation road connecting structure.

The size of boiler is as follows：

The size of-the first catalyst and the second catalyst be 200 × 500 × 120mm (H × W × L), volume For 12,0dm³, treating capacity is 91.700 1/h, and void density is 100cpsi and load is 70g/ft3Pd.

Third catalyst is 200 × 500 × 150mm, and volume is 15,0dm3 and treating capacity is 73.300 1/h.In other respects, specification and the first monomer and second comonomer is identical.

The size of heat exchanger will be 200 × 500 × 300mm, wave height 10mm, plate thickness 0,6mm and material Expect to be 1.4509.

Capacity of heat transmission is calculated with the rated value of 130W/m2oK (rate).

The pressure loss is about 5000Pa, and temperature is equal to the temperature in embodiment before.

If be with the above-mentioned boiler of some other operating fuels it is desirable that, then it is used for the supply in various stages point With must optimize, to optimize capacity of heat transmission.Natural gas has the calorific value of about 50MJ/kg, and light fuel oil has 42,7MJ/kg calorific value, liquefied gas have 46,4MJ/kg calorific value, CO gas with 10MJ/kg calorific value and Ethyl alcohol has the calorific value of 29MJ/kg.

The discharge of flue gas (flue gas) from boiler can use NO among other things_x, SOx, VOC and CO sensing Device monitors.

The option of scheme for being shown in Fig. 3 is a kind of combined-circulation once-through boiler of construction.In this case, similarly, gas In Bottomhole pressure, and water is advanced in the external jacket of pipe.Therefore, catalyst is a vertical row in pipe.(Fig. 2) in order to Enhancing heat is transmitted, and the static mixer that high turbulences are moved can be generated by being provided in pipe.The blade or flight of mixer lead to It crosses the outer surface for being for example soldered to pipe and fastens.This scheme is had already envisaged for for low capacity.For example, the natural gas boiler of 50kW Size will be about D300 × 1500mm.

Above-described embodiment demonstrates catalysis burning and is suitable for the thermal power equipment with all size and capacity.

It as summary above, can be inferred that, it is impossible to be burnt with heat and associated with it for the clear of flue gas Clean method is generated entirely without NO_xThermal energy.The high temperature of heat burning and relatively long duration can all generate NO always_x, should NO_xIt cannot fully be removed later.Here it is the reason of the complete thermal oxide for hindering carbon and hydrogen.Industrial carbon and hydrogen it is complete It is oxidized, without NO_xFormation, can be used only in the catalytic combustion device, Yi Jitong of the utility model run under lower temperature The clean fuel of peroxidating natural gas, biogas, bio-ethanol etc. is realized.In this case, technique will not generate In addition to other noxious emissions of carbon dioxide (CO2), carbon dioxide can be used in the service of the fertilising of such as plant.All cigarettes Road gas can be guided directly into greenhouse, wherein, flue gas is distributed by pipe-line system and is utilized (Fig. 4) by plant.Therefore, cigarette The thermal energy that road gas includes also is utilized.Because additional moisture is harmful for growth, flue gas is being delivered to greenhouse In before, (Fig. 5) can be removed with condensate and heat exchanger in the moisture that flue gas includes.

Outdoor air has the carbon dioxide content of about 380ppm.CO2 fertilisings are realized in vegetable growth greenhouse most Big benefit, wherein, because CO2 concentration is its two times or three times compared with basic horizontal, growth can accelerate up to more In 40%.One it is happy coincidentally, the greenhouse demand of thermal energy and carbon dioxide can pass through carbonoxide in Northern European countries Hydrogen compound and met simultaneously, because of usually harmful titanium dioxide of the generation of necessary thermal energy along with almost amounts of optimization The generation of carbon.CO2 fertilisings can provide remarkable growth on the capacity in greenhouse, thus reduce the energy of production and fund into This.

Finland is characterized as about 1000 companies for being commercialized culture vegetables in the greenhouse.330 utilizations in these companies The liquid of industry manufacture or gaseous CO2.Generally the least expensive liquefied gas cost about 0, the price of 10 euro/kg, and the bottle of most expensive Fill the price that gas spends about 2 euro/kg.It is 4 to 5,000,000 kg/ in the amount of industry manufacture CO2 that Finland uses.It is global to disappear Consumption estimation is more than hundred times.Therefore, not only in terms of greenhouse emissions are reduced, but also in economic aspect, the life in energy production Into carbon dioxide utilization be all high-importance topic.When used fuel is bio-ethanol, synthesis gas or other lifes During object fuel, realizing most significant environment influences.In this case, energy production has negative carbon footprint.Like this It advances, some can also be replaced and given birth to and transported to the CO2 in greenhouse by industrial estate.

If the boiler of the utility model is manufactured to the 1% of boiler for producing covering the whole world, about 1,000 ten thousand are as a result will beCatalyst market.

Claims

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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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. 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.