CN107796009A - The catalytic combustion device for producing the method for the admixture of gas of extremely low discharge and using - Google Patents
The catalytic combustion device for producing the method for the admixture of gas of extremely low discharge and using Download PDFInfo
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- CN107796009A CN107796009A CN201710049930.XA CN201710049930A CN107796009A CN 107796009 A CN107796009 A CN 107796009A CN 201710049930 A CN201710049930 A CN 201710049930A CN 107796009 A CN107796009 A CN 107796009A
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- air
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- combustion
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2202/00—Combustion
- F23G2202/60—Combustion in a catalytic combustion chamber
Abstract
The present invention relates to the method for the admixture of gas for producing extremely low discharge and catalytic combustion device.This method includes at least following steps：Catalytic combustion device (CAB) initial part is supplied to using at least the 90% of the air being catalyzed needed for burning as primary air (AIR1)；Fuel (FU1, FU2, FU3, FU4) is supplied in catalytic combustion device (CAB) at least two successive stages, and the fuel (FU1, FU2, FU3, FU4) that the primary air (AIR1) by being delivered in catalytic combustion device (CAB) initial segment (CAS) is delivered stage by stage at least two successive combustion phases (CA1, CA2, CA3, CA4) with split-level burning；The temperature of the gas (EXG) of generation at least one successive catalysis combustion phases (CA1, CA2, CA3, CA4) is reduced at least one heat transfer stage (HT1, HT2, HT3)；The gas (EXG) of burning generation is removed from combustion apparatus (CAB) final stage (CAL).
Description
Technical field
The present invention relates to the method for the admixture of gas for efficiently producing extremely low discharge in catalytic combustion device.
The invention further relates to the catalysis of the admixture of gas for efficiently producing extremely low discharge using catalytic combustion method
Combustion apparatus.
The invention further relates to the method by using modular manufacture combustion apparatus.
Background technology
The whole world is all in constraint nitrogen oxides (NOx), carbon monoxide (CO), carbon dioxide (CO2) and hydrocarbon row
(VOC) is put, for improvement air quality and for suppressing greenhouse effects.It is right in Europe in order to pursue this target
Heating boiler, process equipment, fireplace etc. have formulated several instructions.Directly or indirectly limited by efficiency in these instructions
Determine to limit for the discharge of fire emission.In the U.S., Bureau for Environmental Protection (EPA) and especially California air resource committee member
The strict standard for nitrogen oxides and hydrocarbon, and some marks for particular compound have been formulated in meeting (CARB)
It is accurate.China is undergoing similar development.30mg/m is had been set in Beijing, such as the NOx of boiler limits value3,
And have been set to 80mg/m for CO limits value3.It is strong identical should also to be continued in other industrial circles of China
Deflationary trend.Because Abgasgesetz becomes increasingly stricter, limitation will be met with by being currently based on the system of heat burning.In addition, tool
The efficiency for having the burner of minimum discharge should decline, because minimum discharge is with the remnant oxygen or flue gas recirculation improved
Come what is realized, and both of which can damage the efficiency of energy production.
In fact, the energy production row known in the state of the art for having several generations for energy and reaching authorities' application
Put the facility of limit value：
- replace rear pass gas disposal, ultralow NOxBurner and without NOxThe manufacturer of burner (Zero NOx burner)
Flue gas recirculation, gas and air classification are make use of in its burner, with technologies such as high excessive air pre-mixing combination burnings.With
Ultralow NOx heat burning can not obtain zero NOxDischarge.In O2During in 3% level, the minimum reported be 5ppm (about
10mg/m3)。
- another option is the purification (purifying) of flue gas.Generally with selective or non-selective catalyst
(SCR, NSCR) realizes the removal of nitrogen oxides.Most preferably, thus about 300 DEG C temperature obtain 98% degree of purification.So
And SCR catalytic converter requires single reducing agent (urea or ammonia) and the distributor for the reducing agent, this cause fuel into
This about 4% ancillary cost.Thus obtained NOxEmission level is about 5ppm to 20ppm.In addition, CO emission limits often will
Seek single oxidation catalytic converter.
- as a kind of new product, market has existed for a kind of 3 effect catalysts by boiler.This is urged
Change converter and do not need reducing agent, but the adjustment of the air/fuel ratio of burner will be subjected to strictly for 3 effect catalysts
Ask.This technology makes it possible to reach for NOxWith CO all existing, even quite strict limits values, but for one
The scheme of kind costly.
It can illustrate as to summary above, the discharge of nitrogen oxides can not pass through heat burning and cigarette associated there
Road gas removal methods are sufficiently decreased to below about 10mg/m3Level and device efficiency without significantly degenerate or invest and
Operating cost does not increase acutely.
As the solution of the problem, some patent applications have been proposed one kind and are divided into two or more stages
Catalysis burning, it is sufficiently low that it will be able to maintain that reaction temperature, to be nearly free from any nitrogen oxides.Such as under
This scheme is disclosed in the patent application in face：GB2295008, US4299192, JPH06288510 and B2077135.It can push away
Survey, the basic combustion plant for forming foregoing invention does not have the technology or commercial terms for being used for starting production also, because all
Above-mentioned application all quite olds, obviously do not obtained also commercially with their the consistent product of description.In these applications
Any one be not present on it is thus having reached or can reaching which kind of discharge detailed description.
These catalysis well known in the prior art for using the catalysis burning including being carried out with two or more stages turn
The combustion apparatus of exchanger technology, has the following problems first：Paint-on technique for being present in catalyst is not enough
Heat-resisting, and it can not make the exploitation of product have competitiveness in price at it.
In addition, the catalyst described in the patent document discussed is all excessive and includes too many noble metal.Begged for
The monomer (unit, cell) of the straight channel catalyst being used in combustion plant described in the patent document of opinion can not be born for a long time
High temperature, especially in the case where uneven temperature is distributed.
Another key problem in catalysis combustion plant discussed above is probably to supply air/fuel mixture
The inconsistency being given in catalyst, this may cause the breaking-up of hot-spot event and catalyst.This is highest in equipment
Operation risk because operation one after the other at the maximum running temperature close to catalyst occur, and because catalyst at it
It is probably big in terms of area of section.Therefore, stream may easily become channelizing.
As summary above, can be inferred that cannot be economical with catalysis combustion plant well known in the prior art
Ground is produced almost without discharge (NOx, VOC and CO) heat energy.
On the other hand, the CO of the discharge gas specifically generated in energy production2Several services can be used in
In, a kind of is that carbon dioxide is used in the carbon dioxide fertilization in greenhouse, by liquefying first or from for energy production
Combustion apparatus is delivered directly to the position used.Carbon dioxide fertilization is most beneficial in vegetables growth.Finland is in truck farm
With 990 greenhouses, and wherein about 330 are used to apply fertilizer using liquid or atmospheric carbon dioxide, about 5,000,000 kilograms altogether/
Year.
In the service for need carbon dioxide using carbon dioxide by simultaneously significantly promotion harmful greenhouse effect mitigation.
In order that the carbon dioxide of the discharge gas generated in energy production can be used in greenhouse for CO2Apply
Fertilizer, it is desirable to which the level for discharging NOx, VOC and CO in gas is very low.Plant is for nitrogen oxides (NOx), oxysulfide
(SOx), hydrogen sulfide (H2S), ethene (C2H4) and CO (referring to following table) than about 100 times of people sensitivity.
The content of the invention
Using prior art above as starting point, first it is an object of the present invention to provide a kind of method and in this method
The middle combustion equipment (equipment, apparatus) used, wherein, energy can be produced with high efficiency and extremely low discharge, without
Burner (arrangement) relative complex known to heat burning is used, or single catalyst wash need not be used
Flue gas.
Secondly, it is an object of the invention to provide a kind of method and the combustion equipment used in the method, wherein, energy can
To be produced with so low discharge so that discharge the CO of gas2It can be used to need in its service, in particular for greenhouse
In carbon dioxide fertilization.
Available combustion apparatus it is yet another object of the invention to provide a kind of catalytic combustion method and wherein, wherein,
A kind of catalysis burning for being divided into two or more stages is employed, but is existed in those no above-mentioned existing known technologies
And heat resistance with catalyst it is associated and prevent this combustion technology it is commercialized serious the shortcomings that.The present invention draws
The scheme especially for the major defect occurred in the above prior art is entered.
The invention allows to reach above-mentioned purpose.Correspondingly, reality is made it possible to according to the catalysis combustion equipment of the present invention
Produce to border without discharge (NOx, VOC and CO) heat energy.In the presence of the ability that heat energy is produced with such low emissions levels, to arrange
Go out the future emission standards that gas meets to tighten.Therefore, the discharge gas CO of generation2Can be used in needs its service
In, such as in the industry as protective gas or in the fertilising in the greenhouse for increasing crop yield.
But clean fuel is used to for these prerequisite, this requires that the fuel cannot include sulphur, nitrogen, halogen
The impurity such as element, silicon, heavy metal.Adoptable fuel includes gaseous state or liquid cleaning fuel, such as natural gas and liquefied gas, low-sulfur
Light oil, alcohols, biogas and biofluid etc..Herein, clean fuel be meant that the fuel include heavy metal,
Silicon, halogen, the organic or inorganic compound of sulphur and nitrogen.In other words, if fuel does not include nitrogen compound, the oxygen of nitrogen is just not present
Generation of compound, etc..
Therefore, the present invention relates to the method for the admixture of gas for producing extremely low discharge in catalytic combustion device.
More specifically, this method is related to the admixture of gas for producing extremely low discharge, and it is related in catalytic combustion device
(CAB) hot recovery in, the catalytic combustion device are included on air (AIR) flow direction in succession the multiple of positioning (successively)
Catalyst, and each catalyst is provided with the hot recovery generated in catalysis is burnt.This method includes：
Admixture of gas (EXC) is prepared by following, average NOx, CO and VOC content of the admixture of gas are burning
Equipment is not higher than 1ppm during being currently running：
- the total air (AIR) that will be used to burn needed for specific fuel quantity (FU) first, primary air (amount) (AIR1)
The first catalyst (CA1) of the combustion apparatus (CAB) on air-flow direction is supplied to, to cause primary air (AIR1)
From the first catalyst (CA1) as auxiliary air (AIR2) proceed at least one other catalyst (CA2, CA3,
CA4), primary air amount is at least the 90% of the total air (AIR),
- by the fuel (FU) needed for catalytic combustion method with least two batches time (FU；FU1, FU2, FU3, FU4) supply
To successive two catalyst (CA on air-flow direction；CA1, CA2, CA3, CA4) in,
- at least two catalyst (CA；CA1, CA2, CA3, CA4) in burning fuel batch (FU1, FU2, FU3,
FU4), at least two catalyst in succession and is mixed catalytic converter on air-flow direction, wherein, due to sky
The flow velocity increase of gas/fuel mixture, the turbulence (turbulency) of air/fuel mixture pass through the primary air
(AIR1) it is enhanced in catalyst,
- at least one heat exchanger (HT；HT1, HT2, HT3) in reduce successive at least two on air-flow direction
Individual catalyst (CA；CA1, CA2, CA3, CA4) in generation gas (EXG) temperature, the heat exchanger (HT；HT1、
HT2, HT3) next catalyst (CA for being positioned on air-flow direction；CA1, CA2, CA3, CA4) upstream, with
And
- the static mixer (MIX) and/or alveolate texture premixer for air/fuel mixture will be to be supplied
To the successive catalyst (CA on air-flow direction；CA1, CA2, CA3, CA4) in primary air or auxiliary air
And fuel batch (FU；FU1, FU2, FU3, FU4) it is directed in the successive catalyst；
At a temperature of not higher than 1100 DEG C, most preferably make in the range of 850 DEG C to 1000 DEG C in combustion method
Fuel (FU) burns, and global fuel burn rate is 0.005s to 0.05s in the combustion apparatus；So as to
The composition of the admixture of gas (EXG) obtained with catalyst is during combustion apparatus is currently running in air stream
The downstream of a final catalyst/multiple catalysts (CA4) on dynamic direction remains unchanged.
Preferably, this method comprises the following steps：Gas recovery mixture (EXG) from the flue of combustion apparatus, and
The admixture of gas is guided to described using position and/or for using position described for heating using position in itself
In carbon dioxide is utilized such as in greenhouse.Correspondingly, therefore it is provided with according to the combustion equipment of the present invention and is included for recovery
Carbon dioxide (CO2) discharge gas (EXC) device, or for the discharge gas to be directed directly into making for such as greenhouse
With the device of position.
The invention further relates to the combustion apparatus used in the method.The combustion apparatus includes being used for two or more
The fuel supply system that batch is supplied fuel in combustion apparatus, for one or more batches will burn needed for air
The air feeder being supplied in the combustion apparatus, be one after the other present on air (AIR) flow direction multiple urges
Change converter, each catalyst is provided with the hot recovery unit for being generated in being burnt in catalysis, and is provided with
The device removed for gas (EXC) will to be discharged from each catalyst.In order to generate its NOx, CO in combustion apparatus
With VOC content not higher than 1ppm and the effluent gas mix carried out in 0.005s to 0.05s time range that burns
(EXC) the upstream also presence for, therefore positioned at primary air flowing at least one catalyst on direction mixes for air/fuel
At least one static mixer and/or alveolate texture premixer of compound so that primary air or auxiliary air and combustion
Charge time can first pass through the blender and/or premixer before they reach at least one catalyst；
- heat recovery units include at least two heat exchangers (HT1, HT2, HT3), two heat exchangers and air flow
Each catalyst of the upstream of next catalyst on direction associatedly positions, and the heat exchanger is designed to
So that provide the temperature for reducing the discharge gas (EXG) generated in successive at least two catalysts on air-flow direction
The ability of degree；
- air feeder is so that first, primary air (amount) (AIR1) can be fed into air-flow direction
In the first catalyst (CA1) of upper combustion apparatus (CAB), to cause primary air (AIR1) from the first catalyst
(CA1) at least one other catalyst is proceeded to as auxiliary air (AIR2), the first, primary air (amount) is burning
A part for total air (AIR) needed for specific fuel quantity (FU), and be at least the 90% of the total air (AIR),
- fuel supply system, thus can be with least two batch quilts in the fuel (FU) needed for catalytic combustion method
Supply in successive two catalysts all on air-flow direction,
- each catalyst is mixed catalytic converter, wherein, because the flow rate of air/fuel mixture
Increase, its enhancing of turbulence in catalyst, it is thus possible that successive at least two being urged on air-flow direction
To change in converter, fuel batch is burnt by the primary air,
- be used to the device that discharge gas removes from catalyst including flue gas passing away, flue gas row
Go out passage to be arranged to be connected with each catalyst, and be preferably coupled to heat recovery units.
The air feeder in this article refer to for forced air be intended to fuel combustion and for air to be drawn
Be directed at catalyst legacy equipment and device in itself.Such device includes such as blower fan (air fan) and prolonged from blower fan
Extend the air conduit of catalyst, and the air distribution device for various air conduits.
Flue gas passing away refers to flue gas discharge conduit, and the flue gas discharge conduit is integrated with heat exchanger and opens
It is put on next catalyst on primary air flowing direction.But the final catalysis in primary air flowing direction turns
The downstream of parallel operation, passing away refers to the flue gas discharge conduit engaged with heat exchanger, or refers to chimney etc., passes through the discharge
The discharge gas that passage generates in combustion apparatus removes from the final stage of combustion apparatus.
For the feedway of fuel such as natural gas, known in Burner Technology set including itself herein
Standby, the equipment is used to establish for the supply pressure of fuel and for the fuel channel by leading to discussed catalyst
Fuel is assigned to catalyst by (especially pipe-line system) with preferable score.Fuel-supplying pressure by pump or fan advantageously
Establish.
Combustion apparatus is currently running the combustion apparatus operation for referring to the beginning and end except burning.
The present invention conceived at present is to be based on catalysis burning being divided into two or more stages (level, stage) first,
But the combustion technology and method applied are based on new scheme, the program makes it possible to avoid what is in the prior art occurred
The problem of being related to catalyst resistance to gentle overheat.
Secondly, the present invention is burnt using catalysis to produce the ability of flue gas based on providing first, and the flue gas can be with
Itself is by for example for heating or carbon dioxide fertilization.Nitrogen oxides (the NO in the discharge gas EG left from catalysis burningx)
Content be less than 1ppm.According to one object of the present invention, one in the discharge gas EXG left by flue etc. from catalysis burning
The content of carbonoxide (CO) is less than 1ppm.According to one object of the present invention, in the discharge gas EXG left from catalysis burning
The content of volatile hydrocarbon (VOC) be less than 1ppm.
In the combustion technology for the combustion apparatus of the present invention, central role is urged by the mixing with static internal structure
Change converter to occupy, for providing attractive cost (flue) admixture of gas with extremely low emission level.
In this disclosure, mixed catalytic converter refers to following catalyst：It has static mixer knot
Structure, and urged in a manner of increasing the flow rate of air/fuel mixture and causing the turbulence of enhancing such a in whole mixing
The each place changed in converter keeps average turbulent air stream.This preferably lives by using very thermostabilization and catalysis
Property coating coating static mixer come perform (by set in catalyst mixed catalyst monomer (unit,
cell))。
In a preferred embodiment of the invention, mixed catalytic converter is the metallic monomer for being equipped with mixed catalyst
(unit), its main body is the static mixer made of steel foil piece (foil sheet), and is coated with catalytically active coatings.
In another preferred embodiment of the present invention, catalyst is provided with new coating, and the coating is height
It is heat-staple and catalytic activity.In this case, catalyst or catalytic domain are coated with by underlying metal (base metal)
Mixed oxide and by noble metal such as Pd and Pt) prepare coating.Noble metal may be constructed the mixed oxidization of parent metal
A part for thing (can be perovskite in configuration aspects).
Catalytically active coatings are made up of the mixed oxide of underlying metal (such as lanthanum, zirconium, tungsten and barium), wherein, such as palladium
It can be used as in being partly comprised in or can individually add with the noble metal of platinum.Mixed oxide can be with its configuration aspects
For perovskite.
This mode, which achieves the advantage that, can prevent the movement of noble metal at high temperature, and avoid noble metal dispersion
The reduction of degree or active noble metals surface area, i.e. prevent the active reduction of catalyst.This set has catalytic activity painting
The catalyst of layer has the expected service life more than 10 years.
According to one object of the present invention, the temperature in each catalysis combustion phases is kept at less than 1100 DEG C, most
Preferably at 850 DEG C to 1000 DEG C.In catalysis oxidation, reaction rate accelerates in two stages.In the temperature with about 350 DEG C
At the first stage of degree, the reaction of dynamics Controlling becomes to be restricted in terms of mass transfer.In the temperature with about 850 DEG C
At second stage, reaction starts to occur on the surface of catalyst.On this temperature, the weight of mixed catalytic converter
The property wanted substantially keeps increasing.Contact between reactant and the surface of catalyst even may have tens times of increasing
Add.
One preferable mixed catalytic converter with static structure is showed such as in such as U.S. Patent application
Construction described in 2008113209.Wherein, catalyst is constructed by oblique ripple steel foil piece, and the oblique ripple steel foil piece is with cross
The ripple of shape pattern stacks or overlapped top of each other.Paillon foil can be fastened to each other in joint, such as pass through electric resistance welding
Or soldering.The circulation road created by each layer of monomer intersected with each other generate with higher flow rate in stream agitation with
Turbulence.
In the monomer of straight channel, stream is laminar flow.Then, in the case where flow rate is 3m/s to 4m/s, represent
Nondimensional Nu Saier (Nu) numbers of mass transfer are 2-3.When flow rate increase, the Nu numbers pole of straight channel slowly increases
Add.As long as flow rate keeps low, hybrid cellular shape or monomer structure are worked as flow rate and increased also without any help of offer
Added-time, Nu numbers exponentially increase, and its mode is：Under 10m/s flow rate, Nu numbers are 8-12, and 20m/s's
Under speed, Nu numbers are 50-100, and this depends on intersecting angle.This size for making it possible to greatly reduce catalyst and your gold
The amount of category, reduces cost and strengthen burning and efficiency.
The hole density of catalyst can be 20-80 holes/cm2(being preferably 30-60), and catalyst
Length can be 25mm to 153mm (being preferably 50mm to 120mm).Increase with the number of pores of catalyst, monomer
Length can be reduced.The paillon foil used in catalyst can be ferrite 1.4767 or have equivalent heatproof (long-term
1200 DEG C) material.Angle between the cross aisle of catalyst can be 25 degree to 50 degree.The structure of catalyst
Similar to the structure in patent application US2008113209.Disclosing on this cellular or monomer structure research SAE
In 2002-01-0357, it was found that in terms of its mechanical endurance relative to other automatic single-bodies (automotive cell) more
Add excellent.
Second important improvement of the combustion technology on being catalyzed combustion plant is used and is located in the present invention
At least one static mixer of the upstream of at least one catalyst on the approach axis of primary air flows.
On be catalyzed combustion plant combustion technology the 3rd important improvement be use in the present invention and position
It is used for air/fuel mixture extremely in the upstream of at least one catalyst on the approach axis in primary air flows
A few premixer.Premixer is generally positioned at the upstream of the blender on primary air flowing direction.Primary air
(AIR1) and fuel (PA) is for fuel-air mixture and positioned at the first catalyst (CA of air-flow direction；
CA1 it is mixed with each other in the alveolate texture premixer (5) of upstream), the flow rate of air and fuel increases wherein.
The static mixer is used to determine that air/fuel mixture is homogeneous (mixing to be combusted in catalyst
Thing), while contributing to the small size of combustion equipment, because burn rate is tens times relative to heat burning, there is no carry
For the needs of the combustion equipment with fuel mixing zone.
Static mixer positioned at catalyst upstream, which preferably includes, to be stacked with cruciform pattern and preferably set
Oblique line (oblique), such as the monomer of the steel disc (steel sheet) of the ripple of sinusoidal shape are equipped with, wherein, oblique ripple piece
Peak is towards opposite direction, so as to which the circulation road of intersection is made, so as to cause the agitation and turbulence in gas.
According to one object of the present invention, the located upstream of each catalyst is possible to be constructed by several parts quiet
State blender.Blender can be constructed by oblique ripple steel band, and wherein ripple prolongs across in a manner of with identical in catalysis monomer
Extend each other.Circulation road by every layer of offer of monomer is intersected with each other, is stirred so as to cause in stream with higher flow rate
And turbulence.The pore-size of blender is more several ten times larger than the pore-size in catalyst.
Static mixer monomer can have 0.2-2 hole/cm2Hole density, and 50mm to 150mm (be preferably
70mm to 100mm) length.The steel band used in monomer can be for the ferrite with 0.2mm to 0.6mm thickness for example
1.4509 or 1.4512.Angle between the cross aisle of blender can be 30 degree to 60 degree.
In the blender of rectangular shape, preferably by two successive monomers so that one mixes in the horizontal direction
And homogeneous flow, and another vertical direction mix and homogeneous flow.
According to one object of the present invention, last catalyst can be bigger than other catalysts, with
Burnt in ensuring to clean.According to fuel and void density, the catalyst of foremost can make its conversion in 80.000 1/h
Change in the range of to 700.000 1/h.In last catalyst, scope can be 60.000 1/h extremely
350.000 1/h。
With the upstream in catalyst existing for the static mixer structure of static mixer and catalyst (set
It is equipped with the catalyst of catalytically active coatings) it is coupled, it likely ensure that the air/fuel mixture of homogeneous and produced in its burning
Constant running temperature, which prevent the hot-spot event in catalyst Anywhere, and therefore protect catalysis
The service life of converter length.
This mode obtains important benefit in the sense：By the catalysis combustion equipment of the present invention, burning can
To be consecutively carried out by using high temperature, it is opposite with existing known arrangement.In addition, the catalytic combustion method developed herein
In, the hot-spot of catalyst can be prevented.
In addition, the mixed catalytic converter structure used in the combustion apparatus of the present invention enables catalyst to reduce
Size, and whole combustion apparatus is reduced size.
Because the ability for producing high-purity flue gas mixture is provided according to the catalytic combustion device of the present invention, therefore institute
Stating admixture of gas (EXC) has NOx, the CO and VOC content for being not more than 1ppm.This enables catalysis combustion equipment in its thermal effect
Upgrade in terms of rate and whole efficiency.
Therefore, in a preferred embodiment of the invention, the efficiency for being catalyzed burning is at least 99.9%, the efficiency quilt
It is calculated as the conversion of the energy that is included in fuel to heat energy.This passes through by heat exchanger existing for being connected with catalyst
Reclaim the energy of burning gases (flue gas) that is generated in catalyst and by using to be guided to making from combustion apparatus
Implemented with (flue) admixture of gas of position to heat using position.Corresponding combustion apparatus is provided with for biology to be fired
Material is supplied to the device in the combustion apparatus, and is provided with for flue gas to be directed directly to especially draw using position
The device into greenhouse is led, for using position with energy heats, and for the CO with flue gas2Heating uses position, by
This used bio-fuel is provided as negative (negative) carbon footprint.
In the case where the whole efficiency of combustion apparatus has increased to about 98%, combustion apparatus be provided with for by
The condensation of the vapor of generation removes the device of vapor in flue gas caused by burning (EXC), and in the condensing unit
Downstream is provided with for flue gas to be supplied in greenhouse for increasing the CO of greenhouse air2The feedway of content.
Removing device by the vapor of condensation includes such as condensed heat exchanger.
Feedway flue gas being supplied in greenhouse includes the pipe-line system of transmission and delivering suitable for gas, and
For increasing the possible fan of flowing pressure.
By the way that the delivering of fuel is divided into two to four-stage, can catalytically oxidizing stoichiometric fuel/sky
Gas mixture.The principle can realize the structure of catalysis oxidation equipment, and catalysis oxidation equipment does not produce nitrogen oxides
(NOx), and carbon monoxide (CO) and hydrocarbon (CH) discharge also all it is extremely low (<1ppm).
The present invention also based on the fact that：When burning is catalytically carried out stage by stage, it can be by using for increasing
The new mixed catalytic converter of strong burning is maintained under LEL (LEL) always.
Therefore another great has an advantage that of above-mentioned catalytic combustion method makes the physical size of catalytic combustion device can
To be significantly smaller than the physical size of the comparable corresponding low emission equipment with heat burning, due to urging in combustion apparatus
Change total burn rate in converter, burn rate specific heat burning is high about 20-50 times and in 0.005s to 0.05s model
In enclosing.
On the other hand, a preferred embodiment of the invention is based in the following manner with multiple successive catalysis turn
Parallel operation carries out the oxidation of fuel so that advances through all catalysis in nearly all or all air needed for oxidation and turns
Parallel operation, but fuel to be oxidized is individually injected into each catalyst by a blender/multiple blenders,
In each catalyst, risen to for a long time more than 1000 DEG C there is no temperature.In a preferred embodiment of the invention, exist
What is inserted between catalyst is preferably heat exchanger, and gas is cooled to by liquid or gaseous medium in the heat exchanger
150 DEG C to 350 DEG C.Fuel to be oxidized is delivered before each catalyst, the oxidized in each catalytic converter
To increase temperature no more than about 1000 DEG C (can also be referring to operation diagrams 1 to 5) again.
In a preferred embodiment of the invention, energy is supplied with the fuel progressively carried out as caused by catalytic combustion device
Fine setting.The change of main performance is carried out by changing the amount of supply air, such as by adjusting the rotary speed of fan.Combustion
The supply of material is according to the temperature control measured after catalyst.
In a preferred embodiment of the invention, heat exchanger is recuperative heat exchanger.Recuperative heat exchanger
It can be used for heating various gaseous states and liquid reagent.In this case, equipment is for example available for heating building thing or industry
The boiler of hot water, steam, hot-air in technique etc..
In a preferred embodiment of the invention, it is temperature sensor after catalyst, in this case
This temperature sensor that the risk of control fuel supply can be used in catalyst downstream is minimized.
On the other hand, itself can be utilized for example for heating or the production of the flue gas of carbon dioxide fertilization
Life brings also unconsummated a variety of benefits.The catalysis combustion equipment of the present invention can be used and produced with clean fuel according to this
The extremely low discharge flue gas of invention；As long as flue gas does not include nitrogen compound, just without generation nitrogen oxide.Therefore, only
Some noxious emission (CO2) can such as in the fertilising in plant, as protective gas, as industrial raw materials by abundant profit
With.
Because the burning gases of catalytic combustion device can be used for the CO in greenhouse in the form of impure2Fertilising, is realized
The benefit that the heat energy included in the burning gases of outflow will be also utilized, so as to combustion apparatus boiler the thermal efficiency rise to it is several
100%.
The energy that the flue gas of the high-purity obtained by the combustion equipment of the present invention makes it possible to both meet greenhouse needs
Ask and meet CO2Fertilising, the growth of vegetables can be strengthened about 40% by this, and be reduced in the heating in greenhouse for extra energy
The demand of amount.Make growing into for hothouse production for producing to utilize close to the increased demand of vegetables using point and increased vegetables
It is inevitable.
In a preferred embodiment of the invention, catalysis combustion equipment can supply its catalyst with various fuel.
The fuel FU supplied can be gaseous state and/or liquid.According to one object of the present invention, the fuel FU supplied be selected from by
The group that natural gas, biogas, liquefied gas, light fuel oil, alcohols and carbon monoxide form.It can also include other flammable gas
Body and liquid.
According to one object of the present invention, fuel is fed into catalytic combustion device at least three successive stages
In CAB, and the fuel supplied stage by stage is by being delivered in catalytic combustion device CAB initial segment (section) CAS
Primary air burns at least three successive catalysis combustion phases.Correspondingly, it is successive on primary air flowing direction
The gas EXG obtained by generation in catalyst is being catalyzed at least two catalysts and accordingly in combustion phases
Temperature reduces at least two heat exchangers, and the heat exchanger is located at the upstream of next successive catalyst.
According to one object of the present invention, fuel is fed into catalytic combustion device with least four successive batch, and
And the fuel supplied stage by stage by be delivered to the first catalyst and catalytic combustion device initial segment primary air with
Mode stage by stage is burnt at least four successive catalysts.Correspondingly, at least two successive catalysis burnings
The flue gas EXG generated in stage temperature reduces at least three heat transfer stages, and the heat transfer stage is positioned at next
The upstream of individual successive catalyst and the accordingly generation of catalysis combustion phases are in catalyst.
According to one object of the present invention, on the total amount of the air needed for catalysis burning, it is not more than it and 10% is used as two
Secondary air is delivered to second catalyst/multiple second of catalytic combustion device in the downstream of the first catalyst
In catalyst.Burning and/or its efficiency are further augmented in this way.
According to one object of the present invention, the flue gas EXG generated in burning temperature is in the final of combustion apparatus CAB
Reduced after the catalysis combustion phases occurred in section CAL catalyst at least one rear heat transfer stage HT4.According to
One object of the present invention, the gas EXG generated in the burning occurred in each catalyst in the heat transfer stage and/or
150 DEG C to 350 DEG C of temperature is cooled in the rear heat transfer stage.
According to one object of the present invention, the heat energy included in the flue gas generated during catalysis is burnt is at least one warm
Reclaimed in transfer stages and/or rear transfer stages, and heat energy is passed to water, air or other liquid or gaseous medium
In.
According to one object of the present invention, the fuel/air rate in the catalysis combustion phases occurred in catalyst
Under LEL (LEL).According to one object of the present invention, the fuel/air rate in combustion phases is catalyzed is LEL
(LEL).
In this disclosure, the air required for during CAB is burnt in catalysis refers to for the complete of used fuel
The amount of the consumed air of burning.It also includes being used to ensure the possible air excess needed for completely burned.The air excess
It can be introduced separately into as primary air or be introduced as primary air and auxiliary air.
Reported the flow direction of section and the order in stage on primary air AIR1.
Unless otherwise indicated, otherwise used average value is 24h average values.
The feelings that the admixture of gas of the stoichiometry used in heat is burnt is almost catalytically aoxidized in the single stage
Under condition, according to model, temperature will rise to about 2500 DEG C because of 20-50 times of higher burn rate.Using according to this structure
Think the equipment of invention, temperature can be by being divided into several stages to maintain the temperature less than 1000 DEG C by oxidation.By more
High burn rate, the size of equipment is than in the extremely low discharge described in the early time the reference small an order of magnitude of equipment of page 1.
It can be used to help, also have with high-precision control and management catalysis burning, auxiliary air by using auxiliary air
Help high efficiency of combustion, the efficiency of combustion is actually 100%.
In view of realizing above-mentioned purpose, the present invention is characterized by the feature presented in independent claims.Other rights
It is required that disclose several preferred embodiments of the present invention.
Principle described in service chart 1 can apply to build a kind of air also to work together with regenerative heat exchanger
Heater.
The combustion apparatus of the present invention has 10kW-100MW performance range.
Brief description of the drawings
Several applications of the present invention are described into Fig. 6 in Fig. 1：
Figure 1A, which is shown, is provided with primary air supply and 2 stage catalytics of secondary air supply and shelltube heat exchanger
Combustion equipment.
Figure 1B, which is shown, is provided with primary air supply and 3 stage catalytics of secondary air supply and shelltube heat exchanger
Combustion equipment.
Fig. 1 C, which are shown, is provided with primary air supply and 4 stage catalytics of secondary air supply and shelltube heat exchanger
Combustion equipment.
Fig. 2 and Fig. 3 shows the static mixing being provided with for primary air and auxiliary air and for fuel supply
3 stage catalytic combustion equipments of device, catalyst and shelltube heat exchanger or fin-tube heat exchanger.
Fig. 4 shows the 3 stage catalytic combustion equipments for making its heat and flue gas be utilized in greenhouse.
Fig. 5 shows the service chart for the combustion apparatus for being provided with the supply of 3 stage fuels.
Fig. 6 shows the upstream for each catalyst on air approach axis that can be arranged in combustion apparatus
The fuel of alveolate texture and the blender of air.
Embodiment
The confession for primary air AIR1 is provided with according to Figure 1A to Fig. 1 C and Fig. 2 to Fig. 3 catalytic combustion device CAB
To device, the feedway is used to introduce catalysis using 90% of the air required for being catalyzed in burning as primary air AIR1
In combustion apparatus CAB initial segment CAS, the initial segment is located at the first mixed catalytic converter CA on primary air flowing direction
Upstream.Primary air feedway includes fan and extends to the initial segment CAS of combustion apparatus air conduit.
The combustion apparatus CAB is additionally provided with fuel supply system, and the fuel supply system is used for will be in primary air flows
Successive 2 to 4 fuel batch FU1, FU2, FU3, FU4 are incorporated into catalytic combustion device CAB on dynamic direction；And it is provided with
2 to 4 successive catalyst CA1, CA2, CA3, CA4, for by being delivered to the initial of (catalysis) combustion apparatus CAB
Primary air AIR1 in section CAS is catalytically burnt fuel FU1, FU2, FU3, the FU4 delivered stage by stage with split-level.
The combustion apparatus is additionally provided with the hot recovery component for being generated in being burnt in catalysis.Recuperation of heat component includes
Heat exchanger HT, the heat exchanger, which has, to be used to reduce at least one gas EXG's for being catalyzed and generating in combustion phases in succession
1-3 heat transfer component HT1, HT2, HT3 of temperature, and described heat transfer component HT1, HT2, HT3 are positioned at next successive
Catalysis combustion phases catalyst CA1, CA2, CA3, CA4 upstream.
The gas EXG generated in catalysis burning removal EXH passes through flue in the final stage CAL from combustion apparatus CAB
Occur Deng (being not shown).Catalytic combustion device CAB after in its final stage, CAL is provided with one heat transfer component HT4 with
For reducing the gas EXG generated in burning temperature after combustion phases CA1, CA2, CA3, CA4 is catalyzed.Cold water WIt is coldQuilt
Guiding is by combustion apparatus for generation hot water WHeatAnd/or warm water WTemperature。
According to Figure 1A to Fig. 1 C and Fig. 2 to Fig. 3, catalytic combustion device is additionally provided with secondary air supply AIR2, and
According to Fig. 2 to Fig. 3, combustion apparatus is additionally provided with least one in each catalyst CA1, CA2, CA3, CA4 upstream
Static mixer MIX.
Fig. 4 shows Fig. 2 catalysis combustion equipment, the gas EXG that is generated in its burning and comprising CO2And hot water
It is utilized in greenhouse Green.
Flow sheet in Fig. 5 is included fuel FU；FU1, FU2, FU3 are with successive on primary air flowing direction
Three stages were supplied in catalytic combustion device CAB, and one by being delivered in catalytic combustion device CAB initial segment CAS
The fuel that secondary air AIR1 is delivered stage by stage in three successive catalyst CA1, CA2, CA3 with split-level burning
FU：FU1、FU2、FU3；Reduce two heat transfer stages HT1, HT2 at least one successive catalysis combustion phases CA1,
The gas EXG generated in CA2, CA3 temperature, described heat transfer stage HT1, HT2 are positioned at next successive catalysis burning rank
Section CA1, CA2, CA3, CA4 upstream；The gas EXG of burning generation is removed from combustion apparatus CAB final stage CAL.Catalysis combustion
Burn equipment CAB its final stage CAL be provided with it is at least one after heat transfer component HT4 for catalyst CA1,
The gas EXG of burning generation temperature is reduced after the catalysis combustion phases that CA2, CA3, CA4 connection perform.Cold water WIt is coldBy
Guiding is by combustion apparatus for generation hot water WHeatAnd/or warm water WTemperature.Catalytic combustion device is additionally provided with secondary air supply
AIR2。
In the equipment of the present invention, the heat exchanger HT of operation can be various recuperative heat exchangers
(recuperative heat exchanger) or recuperative heat exchanger (heat exchanger, regenerative
Heat exchanger), it can be by common boiler or such as 1.4512 and 1.4509 ferrite stainless grade of steel
(stainless ferritic steel grade) is built into.Boiler body can be built by cast recuperative heat exchanger
It is vertical, particularly when medium to be heated is liquid.This embodiment can be performed by two kinds of different principles.According to
Convective principles, water are advanced in pipe, and the burning gases from catalyst release are advanced (Figure 1A to Fig. 1 C) several times outside pipe.
It is desirable using the small pipe of diameter, because so pipe then has relative to the larger external surface area of area of section, therefore from
The heat transfer coefficient of gas to steel is also only about 1/10th relative to the coefficient from steel to water when its highest.
Can by by burning gases develop into turbulent flow it is such a in a manner of pipe is arranged in exchanger to strengthen heat
Transmit.In addition, not only can also be by single steel subregion (steel by flowing deflector wall (flow deflecting wall)
Septal area, steel partition) strengthen heat transfer, the single steel subregion by using enough power from interior expansion pipe and
Pipe is clamped to provide tight metal-contacting surface.Subregion must have enough thickness (1.5mm to 2mm) so that
Its internal heat transfer from gas to steel pipe occurred is effective.Finned tube can also be used, particularly in figs. 2 and 3
In the component of description, for strengthening the heat transfer from gas to metal.
It will be flowed with airtight subregion and be preferably divided into two to four parts, each middle gas in two to four parts passes through
One group of pipeline is advanced once to and fro.Before each part, gas first advances through catalyst.By using burner or
The temperature that catalyst is heated to about 500 DEG C to 700 DEG C by resistance carrys out activation equipment.The placed upstream of each catalyst
There are fuel injection unit and static mixer.It is feasible below：Before catalyst by fuel as far as possible smoothly
Thermal current is transferred to, make it that liquid fuel having time is evaporated and becomes equal in static mixer before catalyst
Mix evenly.
Catalyst CA1, CA2, CA3, CA4 downstream are provided with least one temperature for controlling combustion apparatus to run
Spend sensor.With the increase of power demand, temperature is intended to decline, so as to for example increase the rotation of fan by using frequency converter
Speed carrys out actuating air stream.Based on temperature information, increased in a manner of temperature to be maintained to set such a in the range of limitation
Refuelling supplies.With the decline of power demand, it is also such as to reduce the supply of air and the supply of fuel by temperature control
This.
Final catalyst can have the treating capacity fewer than the catalytic converter of foremost (amount of translation,
Turnover), wherein, according to the type of fuel, treating capacity can change in the range of 80.000 1/h to 70.000 1/h.
In final converter, in order to realize that zero level discharges, treating capacity should be in 60.0001/h to 350.000 1/h.
Equipment can have from small to the capacity greatly changed (capacity), such as 10kW to 100MW.
Two kinds of embodiments of above-described boiler are included below, make design in both embodiments and model calculate with
And sketch 1 and sketch 3.
A kind of design based on modular structure of embodiment 1 and its key dimension and Technology design value are as follows：
- fuel is natural gas.
- with the boiler performance of natural gas it is 50MW.The dosage of natural gas is with the side stage by stage of preferably 40%, 30% and 30%
Formula divides.It is preferably that 1-3% excessively ensures completely burned by a small amount of excess air.
- catalyst is as follows：
The first catalyst and the second catalyst in the primary air direction of the supply be measured as 2600 ×
2600 × 75mm (W × H × L), and there is 507dm3Volume, 108.5221/h conversion, 200cpsi hole density and
40g/ft3Pd load.
Other aspects of 3rd catalyst are all identical, but 2 this converters, total measurement (volume) 1014dm be present3With
And 54,261 1/h conversion.
The 40% of first catalyst injection total amount of fuel, so as to which gas temperature rises to about 850 DEG C from+20 DEG C,
About 250 DEG C are cooled in a heat exchanger simultaneously.
Second catalyst and the 3rd catalyst receive the 30% of fuel, so as to which temperature rises to about 900 DEG C.
- stream of turbulence in a heat exchanger is had been based on, calculated with 100W/m2 ° of K of heat transfer coefficient.
- pipeline is D 40/46mm, and all pipelines there are about 400m, material 1.4512 together.
- external boiler size would is that 3000 × 3000 × 9000mm (W × H × L).
- pressure drop is about 5000Pa.
Described in this paper Figure 1A to Fig. 1 C utilized in the boiler is traditional tubing heat exchanger, wherein, such as
Shown in Figure 1A to Fig. 1 C, water (liquid) is advanced in the duct, and the gas heated is advanced through catalytic conversion to and fro
Device and tubulose honeycomb.
Second of embodiment is shown in figure 3 with dimensional sketch.This boiler is about 5MW with the hot property of natural gas.Combustion
Equipment is burnt by three combustion elements and three heat exchange elements assemblings.Each combustion elements are provided with fuel injection conduit and use
In two static mixers of air/fuel mixture, first of two static mixers is used to mix in the horizontal direction
Through the fluid stream (air+fuel) of blender, and second is used to mix same fluid stream in vertical direction.Each burning member
Part is additionally provided with such as the mixed catalytic converter described in patent US2008113209, and under the mixed catalytic converter
Trip is provided with the temperature sensor for controlling fuel to supply.
Heat exchanger is manufactured by the finned tube welded, in the first stage cooling down burning gases with after second stage
Advanced to about 150 DEG C to 350 DEG C of cooling waters in the finned tube.Phase III includes two identical heat exchangers, passes through
Two identical heat exchanger gas temperatures are reduced to about 120 DEG C.
Each element is provided with inlet duct and outlet conduit for hot liquid to be added.Pipeline is usually to be connected in series
So that cold water flows to its front end, Fig. 2 from the rear end of boiler.Pipeline can also be connected in parallel, thus cause three it is different
Water heating circuit, Fig. 3.
Fig. 3 combustion apparatus can be assembled by the module with bamp joint (flange joint).Outer surface employs
It is heat-insulated.
Combustion equipment has following design：
The size of-the first catalyst and the second catalyst is 700 × 700 × 75mm (H × W × L), and volume is
36,8dm3, 136.000l/h is converted into, hole density 200cpsi, is loaded as 40g/ft3Pd.
- the three catalyst is measured as 2 × (700 × 700 × 75) mm, and with 15,0dm3Volume and
68.000l/h conversion.Equal to the first monomer and second comonomer.
- heat exchanger is measured as 700 × 700 × 500mm.2 this heat are there are in the downstream of last monomer to hand over
Parallel operation.Heat exchanger is manufactured by the finned tube of D30/36mm welding.
- heat exchanger performance is calculated with specified 100W/m2 ° of K.
- pressure drop is about 5000Pa, and temperature is identical with embodiment before.
If it is desire to the fuel assembly described in some other operating fuels, it is used for the supply distribution in independent stage must be most
Goodization, to optimize the heat transfer performance of boiler.Calorific value for natural gas is about 50MJ/kg, the heat for light fuel oil
Be worth for 42,7MJ/kg, the calorific value for liquefied gas is 46,4MJ/kg, the calorific value for CO gas for 10MJ/kg and
Calorific value for ethanol is 29MJ/kg.
The combustion gases exhaust of boiler can use λ, NOx, SOx, VOC and CO sensor and analyzer be monitored.
As summary above, it is inferred that can not possibly be produced with heat burning and flue gas removal methods associated there
Life is entirely without NOxHeat energy.High temperature and relatively long hot firing duration can always produce some and can not be moved completely in the later stage
The NO removedx.Here it is the reason for total thermal oxide of limitation carbon and hydrogen.There is no NOxThe carbon of formation and the industrial complete oxidation of hydrogen are only
Can with the catalysis combustion equipment of the invention run at a lower temperature and by oxidative clean fuel, such as natural gas,
Biogas, bio-ethanol etc. are realized.In this case, technique can utilize except generation in the fertilising of such as plant
Carbon dioxide (CO2) it will not generate noxious emission outside.
Caused all flue gas EXG in combustion apparatus CAB, i.e., can be from combustion apparatus by the flue gas for generation of burning
Chimney etc. greenhouse is guided directly into by pipe-line system, wherein, the flue gas passes through distributing manifold (distribution
Manifold) distribute for being utilized (Fig. 4) by plant.Because excess moisture may hinder to grow, guided by burning gases
Before entering in greenhouse, the moisture included in burning gases can be removed with condensate and heat exchanger.Therefore, except oxygen and water steam
The microscopic residue of gas, burning gases are almost made up of carbon dioxide and nitrogen completely.
When equipment is used to burn bio-fuel, the carbon footprint of greenhouse energy production will be negative (negative).
Fig. 6 shows preferable premixer 5, and the premixer is useful in the combustion apparatus of the present invention and position
In the upstream on primary air AIR1 flow direction being the first catalyst CA.Primary air AIR1 and to be delivered to urging
The fuel PA changed in converter CA is mixed in two stage fuel supply module 50.Described above, fuel supply module
50 position first on air-flow direction is provided with the premixer 5 for air-fuel mixture, and at it
Downstream is provided with static mixer MIX as has been described above close to catalyst CA.Premixer 5 has cellular knot
Structure, and the relative flow of air and fuel is accelerated for air and fuel are thoroughly mixed each other wherein.Then,
Simultaneously occur air distribution (profile) homogenize and the mixing of fuel and air.The operation of premixer monomer 5
Principle be based on make air injection Air1 and fuel inject PA in alveolate texture is pre-mixed each other at a certain angle preferably with
An angle of 90 degrees degree is encountered.It is cellular in premixing for enhancing to the injection rate of alveolate texture premixer 5 to improve fuel PA
In structure 5 and the turbulence on primary air AIR1 flow direction afterwards, and for ensuring that the air-gas of gained mixes
The mixing of compound.Alveolate texture 5 is pre-mixed to come in contrast to the mixing chamber of fuel-air mixture well known in the prior art
Operation, because the operation of the latter is based on the speed for reducing fuel and air and increases its residence time in mixing chamber.
Claims (29)
1. a kind of admixture of gas for being used to produce extremely low discharge and the side hot for the recovery in catalytic combustion device (CAB)
Method, the catalytic combustion device (CAB) are included in multiple catalysts of successive position fixes on air (AIR) flow direction
(CA；CA1, CA2, CA3, CA4), and each catalyst is provided with the hot recovery generated in being burnt to catalysis, its
It is characterised by, methods described includes：
Admixture of gas (EXC) is prepared by following, average NOx, CO and VOC content of the admixture of gas (EXC) exist
Combustion apparatus is not higher than 1ppm during being currently running：
In-the total air (AIR) that will be used to burn needed for specific fuel quantity (FU) first, primary air (amount) (AIR1) supply
In the first catalyst (CA1) for the combustion apparatus (CAB) being given on air-flow direction so that described once empty
Gas (AIR1) proceeds at least one other catalytic conversion from first catalyst (CA1) as auxiliary air (AIR2)
Device (CA2, CA3, CA4), described first, primary air (amount) (AIR1) be at least the 90% of the total air (AIR),
- by the fuel (FU) needed for catalytic combustion method with least two batches time (FU；FU1, FU2, FU3, FU4) supply
To successive two catalyst (CA on the air-flow direction；CA1, CA2, CA3, CA4) in,
- at least two catalyst (CA；CA1, CA2, CA3, CA4) in the burning fuel batch (FU1, FU2, FU3,
FU4), at least two catalyst is successive on the air-flow direction and is mixed catalytic converter,
Wherein, as the flow velocity increase of air/fuel mixture, the turbulence of the air/fuel mixture pass through the primary air
(AIR1) it is enhanced in the catalyst,
- at least one heat exchanger (HT；HT1, HT2, HT3) in reduce successive at least two on the air-flow direction
Individual catalyst (CA；CA1, CA2, CA3, CA4) in generation gas (EXG) temperature, the heat exchanger (HT；HT1、
HT2, HT3) positioned at next catalyst (CA on the air-flow direction；CA1, CA2, CA3, CA4) upstream,
And
- by the static mixer (MIX) and/or alveolate texture premixer for air/fuel mixture, will be to be supplied
To the successive catalyst (CA on the air-flow direction；CA1, CA2, CA3, CA4) in the primary air
Or the auxiliary air is directed to the successive catalyst (CA on the air-flow direction；CA1、CA2、CA3、
CA4 in) and the fuel batch (FU；FU1, FU2, FU3, FU4) it is directed in the successive catalyst；
At a temperature of not higher than 1100 DEG C, most preferably in the range of 850 DEG C to 1000 DEG C, burn in the combustion method
The middle fuel (FU) used, global fuel burn rate is 0.005s to 0.05s in the combustion apparatus, thus
With the catalyst (CA；CA1, CA2, CA3, CA4) obtain admixture of gas (EXG) composition in the burning
Equipment is currently running last catalyst/multiple catalyst (CA4) of the period on the air-flow direction
Downstream remain unchanged.
2. according to the method for claim 1, it is characterised in that the described method comprises the following steps：Institute is reclaimed from flue
State admixture of gas (EXG) and by the admixture of gas (EXG) guiding itself to using position for making described in heating
With position and/or for utilizing carbon dioxide such as in greenhouse in the use position.
3. according to the method for claim 1, it is characterised in that the admixture of gas (EXG) is from the combustion apparatus
(CAB) flue is reclaimed for using the admixture of gas using position.
4. according to the method for claim 1, it is characterised in that existing for being associated with the catalyst (CA)
The energy of heat exchanger (HT) recovery burning gases (EXG) of generation in the catalyst (CA), and pass through
Position is used with treating to guide to the admixture of gas (EXC) heating using position is described from the combustion apparatus, it is described to urge
Change burning with least 99.9% efficiency of combustion, the efficiency of combustion is calculated as the conversion of energy that fuel includes to heat energy
Rate.
5. according to the method for claim 1, it is characterised in that total combustion of the fuel (FU) in the catalyst (CA)
Burning speed is 0.005s to 0.05s.
6. according to the method for claim 1, it is characterised in that have before the catalyst and mixed in air-fuel
Two successive static mixers, first of described two static mixers mix institute in the horizontal direction on compound flow direction
Air-fuel mixture is stated, and another mixes the air-fuel mixture in vertical direction.
7. according to the method for claim 1, it is characterised in that in each catalyst (CA1, CA2, CA3, CA4)
Temperature be not higher than 1100 DEG C, and most preferably in the range of 850 DEG C to 1000 DEG C.
8. according to the method for claim 1, it is characterised in that in the total amount of the air needed for the catalytic combustion method
In be not more than it and 10% be delivered to other catalyst/multiple catalysts as auxiliary air (AIR2)
In (CA2, CA3, CA4).
9. according to any method of the preceding claims, it is characterised in that moved positioned at primary air flows on direction
In the heat exchanger (HT1, HT2, HT3, HT4) in the downstream of the catalyst discussed, will each catalyst (CA1,
CA2, CA3, CA4) in the flue gas (EXG) of generation be cooled to 150 DEG C to 350 DEG C of temperature.
10. according to any method of the preceding claims, it is characterised in that methods described is further comprising the steps of：
Wherein, the heat energy included in the flue gas (EXG) of gained at least one heat exchanger (HT1, HT2, HT3) and/or
Reclaimed afterwards in the heat transfer stage (HT4), and the heat energy is transferred to water, air or other liquid or gaseous medium thereafter.
11. according to any method of the preceding claims, it is characterised in that be delivered to the combustion apparatus (CAB)
In the fuel (FU) be gaseous state and/or liquid, the fuel (FU；FU1, FU2, FU3, FU4) be preferably chosen from by alkane,
The group of alcohols, carbon monoxide composition, the alkane especially natural gas, biogas, liquefied gas, light fuel oil.
12. according to any method of the preceding claims, it is characterised in that each catalyst (CA1,
CA2, CA3, CA4) in catalysis burning to cause to be supplied to the combustion of the fuel-air mixture in the catalyst
The mode that material/air ratio is maintained under LEL (LEL) is carried out.
13. according to any method of the preceding claims, it is characterised in that enter described the one of the combustion apparatus
Secondary air or auxiliary air (AIR) do not allow with the VOC or the content of other combustible gas higher than 20%x LEL.
14. according to any method of the preceding claims, it is characterised in that the primary air (AIR1) and described
Fuel (PA) is mixed with each other in for the premixer of the alveolate texture of the fuel-air mixture (5), the honeycomb
The premixer of shape structure is positioned at the first catalyst (CA on the air-flow direction；CA1 upstream), and its
The flow rate increase of middle air and fuel.
15. a kind of catalytic combustion device being used in the method according to claim 11, the catalytic combustion device is used to produce
Give birth to the admixture of gas (EXC) of extremely low discharge and for reclaiming heat, the combustion apparatus (CAB) includes：For with two or more
The fuel supply system that multiple batches are supplied fuel in the combustion apparatus, for that will be burnt institute with one or more batches
The air needed is supplied to the air feeder in the combustion apparatus, is one after the other present on air (AIR) flow direction
Multiple catalysts (CA1, CA2, CA3, CA4), each catalyst is provided with to burn for reclaiming in catalysis
The hot recovery unit of middle generation and for removing discharge gas from each catalyst (CA1, CA2, CA3, CA4)
(EXC) device, it is characterised in that be currently running the phase in the combustion apparatus to generate average NOx, CO and VOC content
Between be not higher than 1ppm effluent gas mix (EXC)：
- also in the presence of at least one catalyst (CA1, CA2, CA3, CA4) on primary air flowing direction
Upstream at least one static mixer (MIX) of air/fuel mixture and/or the premixer of alveolate texture
(5) so that the primary air or the auxiliary air and the fuel batch (FU) can be reached at them described at least
The blender (MIX) and/or premixer (5) are passed through before one catalyst；
- the heat recovery units include at least two heat exchangers (HT1, HT2, HT3), and at least two heat exchanger is determined
Position is associatedly located at next catalysis into each catalyst (CA1, CA2, CA3, CA4) on the air-flow direction
The upstream of converter (CA2, CA3, CA4), the heat exchanger are designed to make it provide reduction in the air-flow direction
The ability of discharge gas (EXG) temperature of generation in upper successive at least two catalysts (CA1, CA2, CA3, CA4)；
- the air feeder cause thus first, primary air (amount) (AIR1) can be fed into the air stream
In the first catalyst (CA1) of the combustion apparatus (CAB) on dynamic direction so that the primary air (AIR1) is from institute
State the first catalyst (CA1) as auxiliary air (AIR2) proceed at least one other catalyst (CA2, CA3,
CA4), described first, primary air (amount) (AIR1) is burn needed for specific fuel quantity (FU) one of total air (AIR)
Point and for the total air (AIR) at least 90%,
- the fuel supply system causes thus can be with least in the fuel (FU) needed for the catalytic combustion method
Two batches (FU1, FU2, FU3, FU4) are fed into successive two catalysts on the air-flow direction
In (CA1, CA2, CA3, CA4),
- each catalyst (CA1, CA2, CA3, CA4) is mixed catalytic converter, wherein, with the air/fuel
The flow rate increase of mixture, turbulence enhancing of the air/fuel mixture in the catalyst, thus may
, on the air-flow direction in successive at least two catalysts (CA1, CA2, CA3, CA4), fuel batch
(FU1, FU2, FU3, FU4) burns by the primary air (AIR1),
- be used to include flue gas discharge from the middle device for removing discharge gas (EXC) of catalyst (CA1, CA2, CA3, CA4)
Passage, the flue gas passing away is arranged to associate with each catalyst, and is preferably coupled to the recuperation of heat
Unit (HT).
16. catalytic combustion device according to claim 15, it is characterised in that for carbon dioxide (CO will to be included2) row
Go out gas (EXC) to be recovered to using position or for the discharge gas to be directed directly to the device using position, it is described
Use position such as greenhouse.
17. combustion equipment (CAB) according to claim 16, by being assembled for the combustion apparatus (CAB) for removing
The device of the vapor formed in the discharge gas (EXC) that is generated in burning and assembling downstream for will described in
Discharge gas (EXC) is delivered in greenhouse (GREEN) to increase the CO of greenhouse air2The device of content, the combustion equipment
Whole efficiency is promoted to about 98%.
18. the catalytic combustion device (CAB) according to claim 16 or 17, the catalytic combustion device also includes being used to incite somebody to action
Bio-fuel is supplied to the device in the combustion equipment, and for discharge gas (EXG) to be directed directly to use position,
Especially into the device in greenhouse, for using the device and use of position described in the energy heats with the discharge gas
In the CO with the discharge gas2To it is described using position apply fertilizer device, thus used fuel leave negative carbon footprint.
19. combustion equipment according to claim 16, it is characterised in that the catalyst of the combustion equipment
(CA1, CA2, CA3, CA4) by between the catalyst existing heat exchanger (HT) be coupled to realize air each other
Connection, the catalyst (CA1, CA2, CA3, CA4) are successive in primary air flowing direction.
20. combustion equipment according to claim 17, it is characterised in that each on primary air flowing direction
At least one static mixer (MIX) existing for the upstream of catalyst is the mixing for air-fuel mixture
Device, and constructed by oblique ripple shape metal tape and the peak of the band is in contact with each other in joint.
21. the combustion equipment according to any one of claim 17 to 20, it is characterised in that mixed in the air-fuel
On compound flow direction there are two static mixers, described two static mixers in the upstream of the successive catalyst
In one be suitable to mix the air-fuel mixture in the horizontal direction, and another is suitable to described in vertical direction mixing
Air-fuel mixture.
22. the combustion equipment according to any one of claim 17 to 20, it is characterised in that mixed in the air-fuel
The premixer for the air-fuel mixture be present in the upstream of the catalyst (CA) on compound flow direction
(5), the flow rate of the air and fuel increase described in the premixer.
23. the combustion equipment according to any one of claim 17 to 19, it is characterised in that in the air-flow direction
In the static mixer of the upper upstream for being located at the catalyst,
- hole density is 0.2-2 hole/cm2,
Angle between-circulation road is 30 degree to 60 degree,
- metal tape has 0.2mm to 0.6mm thickness, and its material is ferritic steel, such as ferritic steel 1.4509,
1.4512 wait,
- the metal tape has 50mm to 150mm width, it is therefore preferable to 70mm to 100mm.
24. the combustion equipment according to any one of claim 17 to 20, it is characterised in that with the catalyst
In the blender existing for association,
- hole density is 8-50 hole/cm2,
Angle between-circulation road is 25 degree to 50 degree,
- paillon foil has 25mm to a 153mm width, preferably 40mm to 100mm,
- foil material is 1.4767 or the like, and foil thickness is 0.05mm to 0.12mm,
- on the normal operation range of the equipment, Nu Saier (Nu) numbers of representation quality transmission efficiency are relative to traditional straight
The several times or decades of times of passage ceramics or metallic monomer.
25. combustion equipment according to claim 17, it is characterised in that the mixed catalytic converter (CA1, CA2,
CA3, CA4) oxide of underlying metal is coated with, and coated with the coating for including noble metal such as Pd and Pt, wherein, it is described
Noble metal can form a part for mixed oxide, and the mixed oxide can be perovskite in structure.
26. the combustion equipment according to any one of claim 17 to 25, it is characterised in that the heat exchanger is regeneration
Formula heat exchanger and by ferritic steel such as ferritic steel 1.4509 or 1.4512 construct.
27. the combustion equipment according to any one of claim 17 to 26, it is characterised in that the equipment also includes being used for
The device of catalysis burning is monitored and controlled, the device preferably includes λ, NOx, SOx, VOC and CO sensor and analyzer.
A kind of 28. manufacture method for being used for the combustion equipment according to any one of claim 17 to 27, it is characterised in that
For the equipment by module structure, each in the module comprises at least fuel supply system, static mixer, catalytic conversion
Device (CA) and heat exchanger (HT), thus the catalyst (CA1, CA2, CA3, CA4) can be by being included in another mould
Heat exchanger in block is coupled to realize air communication each other.
29. the manufacture method of combustion equipment according to claim 28, it is characterised in that two successive module flanges
Joint is connected to each other, and the bamp joint can be coupled the catalytic conversion of at least successive module by heat exchanger (HT)
Device is to realize air communication each other.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20165668 | 2016-09-07 | ||
| FI20165668 | 2016-09-07 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107796009A true CN107796009A (en) | 2018-03-13 |
Family
ID=61530955
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710049930.XA Pending CN107796009A (en) | 2016-09-07 | 2017-01-20 | The catalytic combustion device for producing the method for the admixture of gas of extremely low discharge and using |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112460612A (en) * | 2020-11-23 | 2021-03-09 | 中国科学院力学研究所 | Diffused gas flameless catalytic combustion sensible heat utilization device |
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| CN105749743A (en) * | 2016-05-04 | 2016-07-13 | 广州高山环境科技有限公司 | Multiphase mixing catalytic oxidation VOCs treatment method and treatment system |
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|---|---|---|---|---|
| CN1067953A (en) * | 1990-11-26 | 1993-01-13 | 催化剂股份有限公司 | The method of fuel mixture sectional combustion |
| JPH06288510A (en) * | 1993-03-31 | 1994-10-11 | Miura Kenkyusho:Kk | Catalyst combustion type boiler system |
| US6289667B1 (en) * | 1996-05-03 | 2001-09-18 | Rolls-Royce Plc | Combustion chamber and a method of operation thereof |
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| CN112460612A (en) * | 2020-11-23 | 2021-03-09 | 中国科学院力学研究所 | Diffused gas flameless catalytic combustion sensible heat utilization device |
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