CN103062779A - Counter flow catalytic combustion method, counter flow catalytic combustor and application thereof - Google Patents
Counter flow catalytic combustion method, counter flow catalytic combustor and application thereof Download PDFInfo
- Publication number
- CN103062779A CN103062779A CN2013100140500A CN201310014050A CN103062779A CN 103062779 A CN103062779 A CN 103062779A CN 2013100140500 A CN2013100140500 A CN 2013100140500A CN 201310014050 A CN201310014050 A CN 201310014050A CN 103062779 A CN103062779 A CN 103062779A
- Authority
- CN
- China
- Prior art keywords
- cavity
- exhaust gas
- organic exhaust
- catalytic
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Incineration Of Waste (AREA)
Abstract
The invention discloses a counter flow catalytic combustion method, a counter flow catalytic combustor and application thereof. The counter flow catalytic combustor comprises a body. An organic waste gas inlet for feeding organic waste gas and a clean waste gas outlet for discharging clean waste gas are arranged on the body. A cavity before catalysis, a first catalytic bed and a cavity after catalysis are sequentially arranged between the organic waste gas inlet and the clean waste gas outlet. The counter flow catalytic combustor has the advantages that the counter flow catalytic combustor is widely applicable and highly practical, heat exchange efficiency is improved, energy is saved, and cost is lowered.
Description
Technical field
The present invention relates to the catalytic combustion technology field, relate in particular to a kind of convection type catalytic combustion method, burner and application thereof.
Background technology
Catalytic combustion technology is being widely used aspect the low-concentration organic exhaust gas processing, VOCs treatment such as chemical industry, automobile and other industries, the gas of colliery air draft is processed, and the burning of the organic volatile in the enamel-covered wire and Btu utilization etc., catalytic combustion technology is one of important means of current atmosphere environmental protection.
The kind of organic exhaust gas is a lot, the different types of organic exhaust gas of catalytic combustion can be selected different catalyst, but all processing procedures need that all organic exhaust gas is heated to corresponding catalysis initiation temperature catalyst combustion reaction could occur, and the organic exhaust gas temperature that enters catalytic bed the efficient of catalytic process and the purifying rate that finally reaches have been determined.Generally speaking, in the temperature range that catalyst can bear, the higher then catalytic efficiency of temperature is higher, and accessible purifying rate is higher.
Therefore, how to utilize the high-temperature gas heating unburned organic exhaust gas still behind the catalytic combustion, become the key that reduces energy consumption and improve purifying rate.In existing catalytic combustion technology, the various defectives of ubiquity: by the low high energy consumption that causes of heat exchange efficiency, back end catalyst low by the catalysis front end temperature front end catalytic efficiency that causes on the low side, that caused by catalysis rear end temperature drift damage, high by the low discharge of poisonous waste concentration that causes of whole catalytic efficiency.
Reverse-flow catalytic combustion is a kind of catalytic combustion technology that is widely studied and applied, and its essence is heat regenerator, and its shortcoming is: need to switch gas flow, cause complicated structure, be unfavorable for manufacturing, operation and the maintenance for the treatment of facility; Each when switching gas flow, enter heat accumulating but not yet entered the organic exhaust gas of catalytic bed, will be discharged as gas after the catalysis, cause intermittent high density pollution discharging, reduced whole clean-up effect.
In addition, using in catalytic combustion is dividing wall type heat exchanger more widely, comprises the dividing wall type heat exchanger of shell-and-tube and the version such as board-like.As everyone knows, the heat exchange efficiency of shell-and-tube heat exchanger is not high.And when using the higher plate type heat exchanger of heat exchange efficiency, usually do not pay attention to the local convection outside the windstream, the unreasonable of design imported and exported and flowed to air-flow, usually so that local convection has upset the operational effect of heat exchanger.Therefore, be necessary to utilize pointedly local convection, optimize the design of plate type heat exchanger.
No matter be heat regenerator, or dividing wall type heat exchanger, heat exchange efficiency all is not so good as direct contact heat exchanger, the temperature of heated gas is reached or near the temperature of exothermal gas.Certainly, unburned organic exhaust gas can not with burning after cleaning exhaust gas carry out mixing heat-exchange, otherwise catalytic combustion can't continue.But at both joints, namely catalytic combustor if can reach in some way the effect of mixing heat-exchange, must improve the front organic exhaust gas temperature of contact catalyst greatly.In addition, if the temperature at two places, catalysis rear end that catalysis front end that organic exhaust gas enters and cleaning exhaust gas leave is approached, whole catalytic process is all carried out under the highest temperature of catalytic efficiency, must improve whole catalytic combustion purifying rate, reduce the remaining content of organics in the cleaning exhaust gas.
As seen, all there is a common defective in heat exchanger of the prior art: hour heat exchanger effectiveness is extremely low for the thermal source of heat exchange and the low-temperature receiver temperature difference, so the ceiling temperature that organic exhaust gas can be heated to significantly is lower than the temperature of the rear gas of burning, can't make the organic exhaust gas temperature significantly be higher than initiation temperature, reach higher catalytic combustion efficient and purifying rate.
Therefore, prior art has yet to be improved and developed.
Summary of the invention
In view of above-mentioned the deficiencies in the prior art, the object of the present invention is to provide a kind of convection type catalytic combustion method, burner and application thereof, be intended to solve the problem that existing catalytic combustion technology catalytic combustion energy consumption is high, efficient is low, purifying rate is low.
Technical scheme of the present invention is as follows:
A kind of convection type catalytic combustion method is used for organic exhaust gas is carried out catalytic combustion, wherein, comprises step:
A, organic exhaust gas is passed into from the organic exhaust gas import is arranged on the front cavity of urging of catalytic bed top top, and be buffered to predetermined speed by the described front cavity flow velocity that organic exhaust gas is downward of urging;
B, the organic exhaust gas that will pass into from the organic exhaust gas import, before described urging, carry out Convective Heating in the cavity with the high-temperature gas that upwards flows after the burning in the catalytic bed, so that the organic exhaust gas before the contact catalyst is heated to predetermined temperature, and the high-temperature gas of the cryogenic gas on catalytic bed top and catalytic bed bottom carried out Convective Heating in the interlayer interval of catalytic bed and hole, to reduce the temperature difference of catalytic bed top and bottom;
Organic exhaust gas after C, control will be heated is passed down through catalytic bed to carry out discharging from the cleaning exhaust gas outlet behind the catalytic combustion.
A kind of convection type catalytic burner, be used for organic exhaust gas is carried out catalytic combustion, wherein, described convection type catalytic burner comprises a burner body, be provided with for the catalytic bed of organic exhaust gas being carried out catalytic combustion at described burner body, be provided be used to cavity before making the downward flow velocity of organic exhaust gas be buffered to urging of predetermined speed on the top of described catalytic bed, the described top of front cavity of urging is provided be used to the organic exhaust gas import that passes into organic exhaust gas; Describedly urge front cavity also to be used for the organic exhaust gas that will pass into from the organic exhaust gas import, before described urging, carry out Convective Heating in the cavity with the high-temperature gas that upwards flows after the burning in the catalytic bed, be used for the organic exhaust gas before the contact catalyst is heated to predetermined temperature; The high-temperature gas of the cryogenic gas on catalytic bed top and catalytic bed bottom carries out Convective Heating in the interlayer interval of catalytic bed and hole, to reduce the temperature difference of catalytic bed top and bottom, also be provided with cleaning exhaust gas outlet on the described burner body, be used for discharging and be passed down through catalytic bed and carry out the cleaning exhaust gas that generates behind the catalytic combustion.
Described convection type catalytic burner, wherein, described catalytic bed is fixed catalytic bed, the catalyst carrier of described fixed catalytic bed is graininess, cellular or silk bulk metal or pottery.
Described convection type catalytic burner, wherein, before described urging the middle part of cavity or before the organic exhaust gas import, be provided with for organic exhaust gas is heated urge before electrothermal tube or gas-operated thermal bath facility.
Described convection type catalytic burner, wherein, the bottom of cavity is provided with for detection of thermocouple before the urging of the organic exhaust gas temperature before the contact catalyst before described urging.
Described convection type catalytic burner, wherein, the described height of front cavity of urging is greater than the minor face width of its level cross-sectionn, and the difference of the horizontal sectional area of described horizontal sectional area of urging front cavity and catalytic bed is in preset range.
Described convection type catalytic burner, wherein, described catalytic bed bottom is provided with one and urges rear cavity, and described cleaning exhaust gas outlet is arranged on described bottom of urging rear cavity.
Described convection type catalytic burner, wherein, described catalytic bed bottom is provided with first and urges cavity, described first urges the side of cavity to be communicated with is provided with second and urges cavity, described second urges the top of cavity to be provided with second catalytic bed of difference in described preset range of horizontal sectional area and catalytic bed horizontal sectional area, the top of described the second catalytic bed is provided with urges rear cavity, and described cleaning exhaust gas outlet is arranged on described top of urging rear cavity.
A kind of application of convection type catalytic burner as described, wherein, the cleaning exhaust gas that adopts the cleaning exhaust gas outlet to discharge heats gas or the liquid that need heat, when heating, adopt the cavity type heat exchanger to carry out heat exchange, described cavity type heat exchanger comprises at least one pair of heat exchange cavity, and each heat exchanging cavity comprises a heat release cavity and is arranged on the heat absorption cavity on described heat release cavity top, is provided with the heat conduction baffle for heat exchange between described heat release cavity and the heat absorption cavity.
The application of described convection type catalytic burner, wherein, when the cavity type heat exchanger comprises many heat exchanging cavity, described many heat exchanging cavity is arranged in order from top to bottom, be provided with the heat conduction baffle for heat exchange between the heat absorption cavity that each heat release cavity is adjacent, described cleaning exhaust gas outlet connects the import of the heat release cavity that is in the top, after cleaning exhaust gas exports the import of the heat release cavity that enters into the top from cleaning exhaust gas, downwards successively by each heat release cavity, discharge from the waste discharge chimney that is communicated with the outlet of the heat release cavity of bottom, the gas that need heat or liquid enter from the import of the heat absorption cavity of bottom, and upwards successively by each heat absorption cavity, being passed into from the outlet of the heat absorption cavity at top needs the destination of using, perhaps when need heating to as if during organic exhaust gas, then directly the outlet of the heat absorption cavity at described top is communicated with organic exhaust gas inlet, to enter into the convection type catalytic burner from described organic exhaust gas import, wherein, the outlet of each heat absorption cavity is arranged on the top of corresponding heat absorption cavity, the outlet of each heat release cavity is arranged on the bottom of corresponding heat release cavity, import and the outlet of each heat absorption cavity, the import of each heat release cavity and the outlet preset distance of all being separated by.
Beneficial effect: the present invention has utilized near the joint of catalytic combustion front and back gas catalytic bed, made the direct heat convection of catalysis front and back gases, greatly improved the temperature of the front gas of catalysis, reduced the work temperature difference of upper strata catalyst and lower floor's catalyst, improved the duty of whole catalyst, improve catalytic combustion efficient, and prolonged catalyst life, greatly be better than existing catalytic combustion device structure.Simultaneously, the present invention is directed to the organic exhaust gas of different relative densities, proposed structure and the method for a catalysis and quadric catalysis, effectively improved organic exhaust gas by the probability of catalytic combustion, improve further the catalytic combustion purifying rate, reduced the pollution of waste gas to atmosphere.In addition, the present invention utilizes the convection properties of gas to propose the cavity type heat exchanger and to the improving one's methods of other heat exchanger structures, has improved heat exchange efficiency, and also the multistage thorough utilization for waste gas residual heat provides channel.Applied range of the present invention has improved heat exchange efficiency, has saved the energy, has reduced cost, has practical characteristics.
Description of drawings
Fig. 1 is the schematic flow sheet of convection type catalytic combustion method of the present invention preferred embodiment.
Fig. 2 is the structural representation of convection type catalytic burner the first embodiment of the present invention.
Fig. 3 is the structural representation of convection type catalytic burner the second embodiment of the present invention.
Fig. 4 is the structural representation of the preferred embodiment of convection type catalytic burner of the present invention and cavity type heat exchanger fit applications.
Fig. 5 is the side view of preferred embodiment shown in Figure 4.
Fig. 6 is that convection type catalytic burner of the present invention and cavity type heat exchanger fit applications are in the structural representation of plural serial stage heated body.
Fig. 7 be convection type catalytic burner of the present invention the application of cavity type heat exchanger and swinging Adsorption Concentration device in conjunction with schematic diagram.
Fig. 8 is the structural representation that convection type catalytic burner of the present invention is used in the heat exchange enamelling machine.
Fig. 9 is the structural representation that convection type catalytic burner of the present invention is used in the hot air circulation enamelling machine.
Figure 10 is the structural representation that convection type catalytic burner of the present invention is used in vertical type enamelling machine.
Figure 11 is the structural representation that convection type catalytic burner of the present invention is used in gas turbine.
The specific embodiment
The invention provides a kind of convection type catalytic combustion method, burner and application thereof, clearer, clear and definite for making purpose of the present invention, technical scheme and effect, below the present invention is described in more detail.Should be appreciated that specific embodiment described herein only in order to explain the present invention, is not intended to limit the present invention.
As convection type catalytic combustion method of the present invention preferred embodiment, as shown in Figure 1, it comprises step:
S1, organic exhaust gas is passed into from the organic exhaust gas import is arranged on the front cavity of urging of catalytic bed top top, and be buffered to predetermined speed by the described front cavity flow velocity that organic exhaust gas is downward of urging;
In the method for this step embodiment, employing is before organic exhaust gas enters the catalytic bed catalytic combustion, a flow velocity of urging front cavity to cushion organic exhaust gas is set first, be buffered to predetermined speed by the described front cavity flow velocity that organic exhaust gas is downward of urging, with the organic exhaust gas that will pass into from the organic exhaust gas import, before described urging, carry out Convective Heating in the cavity with the high-temperature gas that upwards flows after the burning in the catalytic bed, to improve the temperature of the organic exhaust gas before the contact catalyst, specifically as described in the step S2.
S2, the organic exhaust gas that will pass into from the organic exhaust gas import, before described urging, carry out Convective Heating in the cavity with the high-temperature gas that upwards flows after the burning in the catalytic bed, so that the organic exhaust gas before the contact catalyst is heated to predetermined temperature, and the high-temperature gas of the cryogenic gas on catalytic bed top and catalytic bed bottom carried out Convective Heating in the interlayer interval of catalytic bed and hole, to reduce the temperature difference of catalytic bed top and bottom; Then enter step S3.
Organic exhaust gas after S3, control will be heated is passed down through catalytic bed to carry out discharging from the cleaning exhaust gas outlet behind the catalytic combustion.
Core part of the present invention is: by forming the local convection heating with the higher temperatures gas that rises from the bottom from the lower temperature organic exhaust gas of organic exhaust gas inlet, organic exhaust gas before the contact catalyst is heated to predetermined temperature, temperature with the organic exhaust gas before the raising contact catalyst, and make between the higher temperatures gas of the lower temperature gas on catalytic bed top and catalytic bed bottom and form the local convection heating, thereby so that the catalyst in the catalytic bed carries out catalysis under better operating temperature, improve the catalytic combustion efficient of all catalyst, before minimizing is urged, reach higher purifying rate in the heating energy consumption.What must illustrate is, predetermined temperature (being the predetermined temperature of step S2) before described the urging should be significantly higher than initiation temperature, and the rear temperature of urging behind the catalytic combustion also need be lower than the catalyst ceiling temperature, and different and different according to organic exhaust gas and catalyst type of initiation temperature, the ceiling temperature of catalyst then is different according to the catalyst type difference.For example, the organic exhaust gas as leading take dimethylbenzene and cresols, the Production of Enamel Wires that is equipped with simultaneously the ceramic honeycomb palladium-based catalyst is example, initiation temperature is 400 ℃, the ceiling temperature of catalyst is 650 ℃, predetermined temperature before urging so preferably reaches 500 ℃ at least, will guarantee also that simultaneously the rear temperature of urging behind the catalytic combustion is lower than 650 ℃, makes the operating temperature of catalyst between 500 ℃ ~ 650 ℃.
Based on the convection type catalytic combustion method of above-described embodiment, the embodiment of the invention also provides a kind of convection type catalytic burner, as shown in Figure 2.Come convection type catalyticing combustion process of the present invention is elaborated below in conjunction with the convection type catalytic burner.
See also Fig. 2, Fig. 2 is the structural representation of convection type catalytic burner of the present invention preferred embodiment, as shown in the figure, described convection type catalytic burner comprises a burner body 100, be provided with one for the organic exhaust gas import 110 that passes into organic exhaust gas in described burner body 100 upper ends, and the cleaning exhaust gas that is provided with for the discharge cleaning exhaust gas in described burner body 100 lower ends exports 170, between described organic exhaust gas import 110 and cleaning exhaust gas outlet 170, be disposed with urge before cavity 130, the first catalytic bed 150(distinguishes with hereinafter the second catalytic bed, below catalytic bed 150 is referred to as the first catalytic bed 150) and urge rear cavity 160.
Further, before described urging, be provided with for the electrothermal tube 120 that described organic exhaust gas is heated in the cavity 130 and be used for the thermocouple 140 that the temperature to the organic exhaust gas before the catalyst that contacts the first catalytic bed 150 detects, describedly urge front cavity 130 to be positioned at the top of described the first catalytic bed 150.
Preferably, adopt described organic exhaust gas import 110 to be arranged on described front cavity 130 tops of urging, described cleaning exhaust gas outlet 170 is arranged on described bottom of urging rear cavity 160, the described horizontal sectional area of front cavity 130 of urging is greater than the horizontal sectional area of described the first catalytic bed 150, the described height of front cavity 130 of urging is greater than described minor face width of urging front cavity 130 horizontal cross-sections, it is described that to urge the horizontal sectional area of front cavity 130 be the several times of described organic exhaust gas import 110 sectional areas, like this, outside next organic exhaust gas enters from organic exhaust gas import 110 urges front cavity 130, by described buffering of urging front cavity 130, the flow velocity of organic exhaust gas is significantly reduced, and at heat that the organic exhaust gas of the first catalytic bed 150 burning produces so that the first catalytic bed 150 and near gas temperature higher, the gas of higher temperature can produce local convection by colder air with urging front cavity 130 tops, can be heated to predetermined temperature to the organic exhaust gas before the contact catalyst, with the temperature of the organic exhaust gas before the raising contact catalyst.
And organic exhaust gas is after cavity 130 top-down flow velocitys significantly reduce before urging, be not enough to stop the upwards convection current than hot gas, so urge front cavity 130 inside except the flowing downward of organic exhaust gas integral body, make progress than hot gas in a large number in addition, the local convection downward than cold air exists, such convection process can effectively heat the organic exhaust gas of urging in the front cavity 130, thereby the temperature of the organic exhaust gas before the raising contact catalyst, temperature when making organic exhaust gas touch the first catalytic bed 150 is elevated to a predetermined temperature, and (this predetermined temperature is existing the description in preamble, so repeat no more), close to the gas temperature after the catalysis, usually above the catalysis initiation temperature, whole catalyticing combustion process is carried out under the higher temperature of catalytic efficiency, more be conducive to the catalytic combustion of organic exhaust gas.
Embodiment further for the further temperature of raising machine waste gas catalytic combustion, can also arrange one and be used for entering into the front thermal treatment zone of urging that the organic exhaust gas of urging front cavity heats.Specifically can adopt is to urge the outlet of the front thermal treatment zone to connect the organic exhaust gas import of urging front cavity, and, urge the inlet height of the front thermal treatment zone to be set to be lower than the height of urging front cavity, be lower than as far as possible and urge front cavity so that enter the passage of urging before the front cavity or cavity, like this, can not cause hot gas to pour in down a chimney.
Simultaneously, reach the temperature of catalysis ignition for the temperature that guarantees organic exhaust gas, can also before urging, the various heaters such as electrothermal tube or gas-operated thermal bath facility be set the thermal treatment zone, be used for organic exhaust gas is urged front heating, reach the catalysis initiation temperature and get final product stopped heating when the thermocouple of urging front cavity detects organic exhaust gas.
In the invention process, the catalyst of described the first catalytic bed 150 can be fixed catalytic bed, and its carrier is preferably graininess, cellular or silk bulk metal or pottery.When adopting the ceramic honeycomb catalyst, described the first catalytic bed 150 can comprise multi-layer catalyst, wherein, under the effect of gathering of the heat that every one deck catalyst produces, whole downward air-flow is so that the catalyst temperature of lower floor is higher than top, and local convection is so that the heat that lower floor's catalyst produces is upwards mobile, so the temperature difference of each layer catalyst reduces, the temperature difference than the young pathbreaker so that every one deck catalyst all under higher but not too high temperature, work, this convection current catalyticing combustion process is conducive to improve catalytic combustion efficient, is conducive to simultaneously prevent that the catalyst of lower floor from being destroyed by excessive temperature.
Because, if the catalyst operating temperature is excessively low, although its temperature is higher than the catalysis initiation temperature, can make organic exhaust gas generation combustion reaction, because free energy of reaction is not high, catalytic combustion speed is not high yet, namely catalytic combustion efficient is not high.In addition, catalyst operating temperature on the low side also may cause catalyst active center to be stopped up by the unburned deposit, makes the temporary poisoning of catalyst.If the words that the catalyst operating temperature is too high, then might cause the damage of catalyst, this is because the operating temperature of every kind of catalyst has the corresponding upper limit, approaches or the operating temperature that surpasses the upper limit just may cause the damage of corresponding catalyst, causes the catalytic combustion decrease in efficiency.So the convection type catalyticing combustion process among the present invention has reduced the temperature difference of catalyst, both improved catalytic combustion efficient, can prevent that again the catalyst operating temperature is too high damaged.
After organic exhaust gas passes through the first catalytic bed 150 downwards, most organic volatiles of organic exhaust gas all burn into carbon dioxide and water, gas temperature also raises, but according to the height of the relative density of organic exhaust gas, the situation after its burning is also different.
For the organic exhaust gas of relative density less than air, for example only contain or most of be the organic exhaust gas of methane, its unburned part organic volatile molecule also might rise, the catalyst of repeated multiple times contact the first catalytic bed 150 lower floors, so the rear cavity of urging of a larger volume need to be set, for the organic exhaust gas of remnants provides the more again chance of catalytic combustion, as shown in Figure 2, describedly urge rear cavity 160 to be arranged on the bottom of described the first catalytic bed 150, described cleaning exhaust gas outlet 170 is arranged on described bottom of urging rear cavity 160, the difference of the horizontal sectional area of described horizontal sectional area of urging front cavity 130 and the first catalytic bed 150 is in preset range, this preset range should make the horizontal sectional area of urging front cavity 130 be slightly larger than the horizontal sectional area of the first catalytic bed 150, perhaps can make at least the horizontal sectional area of urging front cavity 130 substantially equate to get final product with the horizontal sectional area of the first catalytic bed 150.After the cleaning exhaust gas outlet 170 of organic exhaust gas cavity 160 after urge was discharged, catalyticing combustion process finished, and cleaning exhaust gas can enter into the heat exchanger that needs downwards, perhaps directly is drained in the atmosphere.
As another embodiment of the present invention, for the organic exhaust gas of relative density greater than air, for example contain the organic exhaust gas that produces in the enamel-covered wire of cresols and dimethylbenzene, its unburned heavier organic volatile is to flow downward, so can again not contact with first catalytic bed 150 on top, for this reason, as shown in Figure 3, the cavity of the present invention's the first catalytic bed 150 bottoms is set to first and urges cavity 180, this first urges the side of cavity 180 to be communicated with arranging second to urge cavity 190, the first to urge cavity 180 and second to urge cavity 190 to be collectively referred to as urging cavity.
And urge the top of cavity 190 to be provided with the second catalytic bed 191 described second, the difference of the horizontal sectional area of described the second catalytic bed 191 and described the first catalytic bed 150 is within described preset range, describedly urge rear cavity 160 to be arranged on the top of described the second catalytic bed 191, described cleaning exhaust gas outlet 170 is arranged on described top of urging rear cavity 160, described the first catalytic bed 150 flushes with the bottom of described the second catalytic bed 191, described first urges cavity 180 to urge the bottom of cavity 190 to flush with described second, the catalyst number of plies of described the first catalytic bed 150 is Duoed 1 ~ 3 times than the catalyst number of plies of described the second catalytic bed 191, describedly urges front cavity 130 to flush with the described top of rear cavity 160 of urging.First urges cavity 180 and second to urge the volume of cavity 190 needn't be excessive, can gather too much heavier organic volatile molecule in the cavity otherwise urge.Wherein, urge the height of rear cavity 160 suitably to increase, like this behind the catalytic combustion through the first catalytic bed 150, remaining organic exhaust gas arrives urges cavity, and after again burning through the second catalytic bed 191, enter into and urge rear cavity 160, remaining organic exhaust gas reduces again.And after urging in the cavity 160, because flow velocity is less, heavier organic volatile molecule also has the trend of sinking, the organic volatile molecule that sinks also can multiple-contact the second catalytic bed catalyst, multiple-contact brings repeated combustion, and this will improve the catalytic combustion efficient of the larger organic exhaust gas of relative density greatly.In Production of Enamel Wires, both comprised inflammable solvent evaporates thing in the organic exhaust gas, such as dimethylbenzene and cresols etc., also comprised nonflammable low molecule paint volatile matter, such as polyurethane or polyester etc.The solvent evaporates thing of dimethylbenzene and cresols and so on all is carbochain less than 10 hydrocarbon, and the gaseous state relative density is about 3.5 ~ 4, and can directly burn under catalyst action, by reaching preferably clean-up effect with upper type.For the paint of polyurethane or polyester and so on, should become the solid-state paint film of enamelled wire surface after the cross-linking reaction, but at high temperature have the short low molecule paint of part strand can change gaseous state into, enter catalytic combustor with solvent.Although the strand of low molecule paint volatile matter is relatively short in paint, but the carbochain than solvent is much bigger, so its gaseous state relative density is also much bigger, and under catalyst action, can not directly burn, progressively cracking could be by catalytic combustion, so need higher temperature and long reaction time after arriving less carbochain.In the cavity, overweight low molecule paint volatile matter is difficult to arrive the cleaning exhaust gas outlet, can rest on for a long time near the second higher catalytic bed of temperature, has more chance to be cracked into short carbochain, and burns into carbon dioxide and water after the urging of above structure.Except enamel-covered wire, the organic exhaust gas of similar this situation is also a lot, as automotive lacquer, furniture spray paint, tire production etc.Common way is: before organic exhaust gas enters catalytic combustion, with methods such as sprays the nonflammable material in the organic exhaust gas is washed off first, thereby brought again the problem of sewage disposal.If contained nonflammable material is the hydrocarbon of cleavable and final burning in the organic exhaust gas, adopt above structure can save the spray program, directly process clean by catalytic combustion.
In addition, because cleaning exhaust gas outlet 170 is arranged on the top of urging rear cavity 160, so cleaning exhaust gas is discharged from this cleaning exhaust gas outlet 170 after the burning, and heavier organic volatile molecule is less, the pollution level of emission gases further reduces, and after discharging from this cleaning exhaust gas outlet 170, the catalyticing combustion process of organic exhaust gas all finishes, can enter into heat exchanger downwards, perhaps directly upwards enter in the atmosphere.
What must illustrate is, above-mentioned design is example more preferably just, do not represent limitation of the present invention, larger urge rear cavity to make heavier organic volatile molecule and following the second catalytic bed carry out repeatedly catalytic combustion if adopt principle of the present invention namely to arrange one, can realize purpose of the present invention equally.
In addition, the catalyst number of plies of the first catalytic bed 150 should be Duoed 1 ~ 3 times than the catalyst number of plies of the second catalytic bed 191, so that total catalyst number of plies reaches air speed than the sum that requires.
From the above-mentioned cleaning exhaust gas of discharging the rear cavity of urging, it contains a large amount of heats, and in order effectively to utilize these heats, the present invention can be applied in the convection type catalytic burner in the various heat-exchange devices.
Specifically, in conjunction with Fig. 4 and shown in Figure 5, be convection type catalytic combustion implement body Application Example of the present invention, be the preferred embodiment of cavity type heat-exchanger rig, as shown in Figure 4 and Figure 5, the cavity type heat exchanger 200 that it comprises above-mentioned convection type catalytic burner and is connected in this convection type catalytic burner, described cavity type heat exchanger 200 is connected to the below of described convection type catalytic burner, described cavity type heat exchanger comprises at least one heat exchange cavity, each heat exchange cavity comprises a heat release cavity 220 and a heat absorption cavity 210(for convenience of description, only identify the heat release cavity 220 and the heat absorption cavity 210 that are in the top among the figure, other heat exchange cavitys are by the same way as setting), in each heat exchange cavity, heat release cavity 220 is positioned at the bottom of heat absorption cavity 210, and, be separated by by heat conduction baffle 230 between heat release cavity 220 and the heat absorption cavity 210, this heat conduction baffle 230 is as main heat-transfer surface, also can fin heat absorbing sheet and fin be set at this heat conduction baffle 230, the volume of heat release cavity 220 and heat absorption cavity 210 and sectional area need enough large, gas so that entering into flow velocity behind the heat exchange cavity, gas is significantly smaller than flow velocity in the passage, so that can produce sufficient convection current in the heat exchange cavity.
It is the specific embodiment of fit applications how that the below specifically describes convection type catalytic burner and cavity type heat exchanger.
As shown in Figure 4 and Figure 5, described cleaning exhaust gas outlet 250 connects the import of the heat release cavity 220 that is in the top, cleaning exhaust gas enters into the import of heat release cavity 220 at top from cleaning exhaust gas outlet 250 after, downwards successively by each heat release cavity, discharge from the waste discharge chimney that is communicated with the outlet of the heat release cavity of bottom, the gas that need heat or liquid enter from the import of the heat absorption cavity of bottom, and upwards successively by each heat absorption cavity, being passed into from the outlet of the heat absorption cavity 210 at top needs the destination of using, perhaps when needing heating target to be organic exhaust gas, then directly the outlet of the heat absorption cavity 210 at described top is communicated with the organic exhaust gas import of convection type catalytic burner, carries out catalytic combustion to enter into the convection type catalytic burner from described organic exhaust gas import.
In addition, the outlet of heat release cavity 220 should be arranged on the bottom of this heat release cavity 220, and the import of heat release cavity 220 is exported away from it, perhaps adopt baffle plate that import and outlet are separated, to guarantee leaving at first heat release cavity 220 through colder exothermal gas after the convection current.The outlet of heat absorption cavity 210 is arranged on the top of this heat absorption cavity 210, and make the heat absorption cavity 210 outlet away from its import, perhaps also can adopt baffle plate to separate import and outlet, guarantee to leave at first heat absorption cavity 210 through hotter endothermic gas after the convection current, in addition, the outlet of described heat absorption cavity 210 is communicated with described organic exhaust gas import, and the import of described heat release cavity 220 is communicated with described cleaning exhaust gas outlet, and gas flow is referring to accompanying drawing 4 and Fig. 5.
When more heat exchanging cavity is set, every heat exchanging cavity sets gradually from top to bottom, enter in the heat release cavity 220 of exothermal gas by the superiors, successively flow to the heat release cavity of foot by interface channel, and leave the cavity type heat exchanger by the heat release cavity of foot, endothermic gas is entered by the heat absorption cavity of foot, successively flows to the heat absorption cavity 210 of topmost by interface channel, and leaves the cavity type heat exchanger by the heat absorption cavity of topmost.And heat conduction baffle is set also between the heat exchange cavity, the top of the heat conduction baffle between the heat exchange cavity is the exothermal gas of last layer heat release cavity, the bottom is the endothermic gas of lower one deck heat absorption cavity, both temperature difference are less, it is less important heat-transfer surface, less important heat-transfer surface is traditionally arranged to be simple heat conduction baffle and gets final product, but also can fin heat absorbing sheet and fin be set at this less important heat-transfer surface.
Between the heat release cavity and between the heat absorption cavity, come circulated gases by interface channel, the form of interface channel can be made as various shape, for example when less demanding to exothermal gas and endothermic gas form, the interface channel of exothermal gas stream circulation can be set in the front of cavity type heat exchanger, the interface channel of endothermic gas circulation usefulness is set simultaneously, with the situation of avoiding passage to intersect in the side of cavity type heat exchanger.If the present invention is applied in the enamel-covered wire, because this situation requires the fresh air of cavity type heat exchanger output to be evenly distributed in flat channel, require simultaneously to extract equably with flat channel and urge rear gas, the interface channel that this moment can the cavity type heat exchanger is set to the uniform orthogonal channel in interval.In addition, the cross section of all interface channels should be enough large, in order to avoid circulating resistance is excessive, the dividing plate between interface channel and the heat exchange cavity, and the dividing plate between interface channel and the interface channel, can be as the auxiliary heat-exchanging face, have equally heat exchange function, like this, in the situation of using same material and heat exchange area, can reach best heat exchange effect, and keep the condition of further utilizing the exothermal gas waste heat.
Among the present invention, after aforesaid exothermal gas refers to that institute's heat content is utilized, finally will be discharged to the waste gas of atmosphere, for catalytic combustion, just refer to that most of organic volatile burns, oxygenous greatly reducing, and contain more carbon dioxide and water, can't enter into again the low pollution waste gas of operation, for example the cleaning exhaust gas behind the catalytic combustion.Aforesaid endothermic gas need in the operation to refer to use, and needs before use the gas that heats, can be the organic exhaust gas that contains organic volatile, also can be fresh air or other gas that needs in the operation.
The kind of the endothermic gas by the cavity type heat exchanger can also surpass a kind of in addition, when if the temperature that multiple endothermic gas requires is all had relatively high expectations, flow will be restricted, at this moment, can adopt mode in parallel to share the heat absorption cavity, when the temperature contrast that requires when multiple endothermic gas is larger, then can share by the mode of series connection the exothermal gas liberated heat of different temperatures, i.e. classification heat exchange.In the classification heat exchange, the endothermic gas that temperature requirement is higher, perhaps identical the and more important endothermic gas of temperature requirement absorbs heat by the heat absorption cavity near the upper strata.When the flow of endothermic gas keeps fixedly, can not control it this moment by the temperature of cavity type heat exchanger, so need to guarantee by the mode of supplementary heating the temperature that endothermic gas reaches to be needed, and the flow of endothermic gas is can change the time, the flow that then can strengthen endothermic gas reduces its temperature, perhaps promote temperature by the flow that reduces endothermic gas, namely control temperature after the endothermic gas heat absorption by the flow of control endothermic gas.
Certainly, during practical application, be not only that gas needs heat, other forms of fluid also might need heat, liquid for example, such as domestic hot-water or steam etc., can use the cavity type heat exchanger this moment according to same principle, as shown in Figure 6, organic exhaust gas enters from organic exhaust gas import 340, through generating clean waste gas behind the catalytic combustion of convection type catalytic burner, cleaning exhaust gas is discharged by the cleaning exhaust gas outlet 310 of the heat release cavity of basecoat, cold water is then entered by the need heat air liquid-inlet 320 of basecoat heat absorption cavity bottom, hot water after the heating is flowed out by the need heat air liquid outlet 330 at last layer heat absorption cavity top, and larger cavity volume has stored considerable hot water, and the continuous operation of catalytic combustion can guarantee continuous hot water supply, only the temperature of hot water will be inversely proportional to the flow of hot water, the hot water thermal insulating tank also should be set when the hot water temperature is had relatively high expectations independently or carry out follow-up heat treated.
Cavity heat exchanger among the present invention is compared with the heat exchanger of some other series connection, its fluid resistance is little, there is not the limited problem of fluid flow yet, when heat exchanger volume of the present invention is limited, then can not use the cavity type heat exchanger, and directly the heat exchanger of existing board-like, plate-fin or shell-and-plate is carried out structure of modification, to reach preferably heat transfer effect.
When organic exhaust gas concentration is lower or unstable, can desorbs technique by absorption and improve organic exhaust gas concentration, for catalytic combustion creates favorable conditions.Use large cavity type heat exchanger heats fresh air, as desorbing thermal current, solution enters the cavity type heat exchanger after being attached to concentrated organic exhaust gas to the fresh air after the heating again, then enters convection type catalytic combustion operation again.As shown in Figure 7, organic exhaust gas passes into from organic exhaust gas import 440, after hot fresh air enters from hot fresh air inlet 460 simultaneously, cavity type heat exchanger and the heating that desorbs electrothermal tube 420 have been passed through, pass into first the passage that desorbs of swinging Adsorption Concentration device 410, solution enters the cavity type heat exchanger after being attached to concentrated organic exhaust gas again, then enters and urges front cavity, discharge from cleaning exhaust gas outlet 470 at last, fresh air is also discharged from cleaning exhaust gas outlet 450.Desorb passage and interface channel thereof and all be provided with heat-insulation layer, the thermal control target that adds that desorbs electrothermal tube 420 is to guarantee to desorb the temperature that thermocouple 430 records to reach the optimum solution enclosure temperature.The concentrated organic exhaust gas that solution is attached to still can urge front temperature to reach the catalysis initiation temperature by urging front electrothermal tube supplementary heating, making after entering the heating of cavity type heat exchanger again.
When the organic exhaust gas concentration of needs absorption was low, being used for the hot fresh air flow that desorbs should be less than the organic exhaust gas flow of needs absorption, made to separate attached organic exhaust gas concentration and be in higher but be not higher than the concentration level of fire point.When the organic exhaust gas concentration of needs absorption or instability of flow, cooperates with swinging Adsorption Concentration device, should adopt the frequency control blower fan to control for the hot fresh air flow that desorbs.When the organic exhaust gas concentration of needs absorption or flow were on the low side, lengthened the gyration period of swinging Adsorption Concentration device 410, reduces simultaneously hot fresh air flow, makes catalytic combustion be in the low cruise state.When the organic exhaust gas concentration of needs absorption or flow were higher, shortened the gyration period of swinging Adsorption Concentration device, improves simultaneously hot fresh air flow, makes catalytic combustion be in the high-speed cruising state.So, can make to greatest extent catalytic combustion be in the self-heating running status, the energy consumption when reducing organic exhaust gas caloric value deficiency further reduces the resistance that green technology is used.
As shown in Figure 8, Fig. 8 is the structural representation that convection type catalytic burner of the present invention is used in the heat exchange enamelling machine, organic exhaust gas passes into from the organic exhaust gas import 510 in left side, directly enter into the convection type catalytic burner and carry out catalytic combustion, the cleaning exhaust gas that generates is by the heat release of a plurality of heat release cavitys, cleaning exhaust gas from the right side goes out 520 mouthfuls of upwards discharges at last, fresh air then enters into the heat absorption cavity of cavity type heat exchanger from the cold fresh air inlet 530 on right side, through discharging from hot fresh air outlet 540 after the heating of electrothermal tube, lead to burner hearth.
For the higher organic exhaust gas of initial temperature, such as the organic exhaust gas in the enamelling machine, even its temperature a little less than the catalysis initiation temperature, because of the Convective Heating effect of convection type catalytic combustion, can not arrange heat exchanger and heat organic exhaust gas.At this moment, the heat of gas can be used for other purpose after the catalysis, for enamelling machine, at first is exactly to heat fresh air supply burner hearth, reduces the energy consumption of preheat fresh air.As shown in Figure 8, gas all enters the cavity type heat exchanger after the catalysis of heat exchange enamelling machine, discharges behind the heating fresh air.Warmed-up fresh air in the cavity type heat exchanger, leads to burner hearth and uses after temperature required through the electrothermal tube supplementary heating.The flow of fresh air makes the interior gas flow of burner hearth close to balance close to the organic exhaust gas flow at this moment, reduces the flow that fire door enters cold air.
As shown in Figure 9, Fig. 9 is the structural representation that convection type catalytic burner of the present invention is used in the hot air circulation enamelling machine, different from the heat exchange enamelling machine is, a gas part is recycled blower fan and draws back burner hearth after the catalysis of hot air circulation enamelling machine, remaining just by the discharge of cavity type heat exchanger, as shown in Figure 9, the convection type catalytic burner is arranged on the left side (preferred embodiment) of cavity type heat exchanger, after organic exhaust gas enters from the organic exhaust gas import 610 of cavity type heat exchanger, enter into the convection type catalytic burner by the cavity type heat exchanger and carry out catalytic combustion, a cleaning exhaust gas part that generates behind the catalytic combustion is recycled blower fan from circulating air outlet 630 and draws back burner hearth, and a remaining part is discharged from cleaning exhaust gas outlet 620 by the cavity type heat exchanger.This moment, the organic exhaust gas flow equaled circulating air flow and combustion gas flow sum.Usually the hot air circulation enamelling machine does not need hot fresh air, and the cavity type heat exchanger still is used for the heating organic exhaust gas, so the exothermal gas flow of participation heat exchange is less than the endothermic gas flow.The time that the exothermal gas that flow is less stops in the cavity type heat exchanger is longer, and the temperature when discharging from cavity type heat exchanger bottom closer to the organic exhaust gas temperature that is passed into by the bottom, can be utilized its waste heat better.And will higher through the organic exhaust gas temperature of heat exchange, higher urge front temperature to be conducive to improve urging rear temperature, thereby remedy the organic exhaust gas concentration reduction that the air circulation of larger flow brings, and the catalytic combustion temperature rise problem on the low side that causes.
As shown in figure 10, Figure 10 is the structural representation that convection type catalytic burner of the present invention is used in vertical type enamelling machine, and the optimal design of vertical type enamelling machine also is a kind of hot air circulation enamelling machine, and difference is the putting position difference.Because vertical type enamelling machine short transverse spatial constraints is less, so the convection type catalytic burner is arranged on the top, arranges downwards successively and urge the front thermal treatment zone and cavity type heat exchanger.
Organic exhaust gas enters from the organic exhaust gas import 710 of cavity type heat exchanger, by the cavity type heat exchanger, again through urging the front heating of urging of the front thermal treatment zone, enter at last the convection type catalytic burner and carry out catalytic combustion generating clean waste gas, wherein, the cleaning exhaust gas of a part is recycled blower fan from circulating air outlet 730 and draws back burner hearth, and remaining cleaning exhaust gas then is passed into downwards in the cavity type heat exchanger, discharges from the cleaning exhaust gas outlet 720 of bottom.Since vertical type enamelling machine to urge front heating power to require larger, urge the volume of front cavity may be not enough to install abundant electrothermal tube, so need special the setting urge the front thermal treatment zone, urge the front thermal treatment zone and urge front cavity that electrothermal tube can be installed simultaneously.Such arrangement mode is conducive to heat is retained in the enamelling machine most, and good controllability also is provided simultaneously.
In above-described horizontal and vertical enamel-cover roasting oven, when overall heat is less, can suitably reduce the waste discharge flow, strengthen the ratio of circulating air, reduce energy consumption.This moment, corresponding organic exhaust gas concentration was usually lower, and the oxygen-content reduction amplitude of circulating air is little, can too not affect Catalytic Combustion Effect.When organic exhaust gas concentration is higher, when causing overall heat more, can strengthen the waste discharge flow, reduce the ratio of circulating air, make the level that each technological temperature is reduced to be needed.Heating energy consumption this moment can be close to zero, and the fresh air of large flow can guarantee the required oxygen of catalytic combustion.
As shown in figure 11, its structural representation of in gas turbine, using for convection type catalytic burner of the present invention.Catalytic combustion produces urges rear gas temperature generally about 600 degree, is extraordinary gas turbine power generation thermal source.There is not special purposes for burner exhaust heat, and the comparatively sufficient situation of waste heat generation, such as the biogas of Sewage Disposal, the gas in colliery, the occasions such as tail gas of fuel cell, can cooperate gas turbine generator to generate electricity.
As shown in figure 11, at first, after organic exhaust gas passed into from organic exhaust gas import 810, utilize the compressor 820 of gas turbine that organic exhaust gas is pressurizeed; Then, the heat absorption cavity that the organic exhaust gas after the pressurization is passed into the cavity type heat exchanger heats, and this moment, the pressure and temperature of organic exhaust gas all raise to some extent.Then, the organic exhaust gas after the pressurized, heated passed into carry out catalytic combustion in the convection type catalytic burner, the organic matter in this moment organic exhaust gas is converted into carbon dioxide and water, and organic exhaust gas becomes cleaning exhaust gas, and the pressure and temperature of cleaning exhaust gas is all significantly raise.The cleaning exhaust gas of HTHP enters the turbine 830 of gas turbine, drives generator 850 runnings and the generating of gas turbine.The cleaning exhaust gas that has discharged pressure in gas turbine passes into the heat release cavity of cavity type heat exchanger again, is used for the organic exhaust gas after heating is pressurizeed.At last, most of heat has been passed on to the cleaning exhaust gas temperature of the organic exhaust gas after the pressurization not high, content of organics is also very low, can be directly be disposed to the atmosphere from the cleaning exhaust gas outlet 840 of bottom heat release cavity, also can be used further to heat again discharging behind the domestic hot-water.
In sum, the present invention has utilized near the joint of catalytic combustion front and back gas catalytic bed, made the direct heat convection of catalysis front and back gases, greatly improved the temperature of the front gas of catalysis, reduce the work temperature difference of upper strata catalyst and lower floor's catalyst, improved the duty of whole catalyst, improved catalytic combustion efficient, and prolonged catalyst life, greatly be better than existing catalytic combustion device structure.Simultaneously, the present invention is directed to the organic exhaust gas of different relative densities, proposed structure and the method for a catalysis and quadric catalysis, effectively improved organic exhaust gas by the probability of catalytic combustion, improve further the catalytic combustion purifying rate, reduced the pollution of waste gas to atmosphere.In addition, the present invention utilizes the convection properties of gas to propose the cavity type heat exchanger and to the improving one's methods of other heat exchanger structures, has improved heat exchange efficiency, and also the multistage thorough utilization for waste gas residual heat provides channel.At last, in several application cases, understand specifically application of principle and method, make catalytic combustion technology reach better effect in existing application, also can significantly reduce simultaneously the threshold values of its self-heating operation, so that the original higher operating mode of operating cost can significantly reduce operating cost, even bring extra returns, and reduce the resistance that enterprise adopts environmental protection technique, promoted the environmental protection cause development.
Should be understood that application of the present invention is not limited to above-mentioned giving an example, for those of ordinary skills, can be improved according to the above description or conversion that all these improvement and conversion all should belong to the protection domain of claims of the present invention.
Claims (10)
1. a convection type catalytic combustion method is used for organic exhaust gas is carried out catalytic combustion, it is characterized in that, comprises step:
A, organic exhaust gas is passed into from the organic exhaust gas import is arranged on the front cavity of urging of catalytic bed top top, and be buffered to predetermined speed by the described front cavity flow velocity that organic exhaust gas is downward of urging;
B, the organic exhaust gas that will pass into from the organic exhaust gas import, before described urging, carry out Convective Heating in the cavity with the high-temperature gas that upwards flows after the burning in the catalytic bed, so that the organic exhaust gas before the contact catalyst is heated to predetermined temperature, and the high-temperature gas of the cryogenic gas on catalytic bed top and catalytic bed bottom carried out Convective Heating in the interlayer interval of catalytic bed and hole, with the temperature difference of a reducing top and bottom;
Organic exhaust gas after C, control will be heated is passed down through catalytic bed to carry out discharging from the cleaning exhaust gas outlet behind the catalytic combustion.
2. convection type catalytic burner, be used for organic exhaust gas is carried out catalytic combustion, it is characterized in that, described convection type catalytic burner comprises a burner body, be provided with for the catalytic bed of organic exhaust gas being carried out catalytic combustion at described burner body, be provided be used to cavity before making the downward flow velocity of organic exhaust gas be buffered to urging of predetermined speed on the top of described catalytic bed, the described top of front cavity of urging is provided be used to the organic exhaust gas import that passes into organic exhaust gas; Describedly urge front cavity also to be used for the organic exhaust gas that will pass into from the organic exhaust gas import, before described urging, carry out Convective Heating in the cavity with the high-temperature gas that upwards flows after the burning in the catalytic bed, be used for the organic exhaust gas before the contact catalyst is heated to predetermined temperature; The high-temperature gas of the cryogenic gas on catalytic bed top and catalytic bed bottom carries out Convective Heating in the interlayer interval of catalytic bed and hole, to reduce the temperature difference of catalytic bed top and bottom, also be provided with on the described burner body and be passed down through catalytic bed for discharge and carry out the cleaning exhaust gas that generates behind the catalytic combustion.
3. convection type catalytic burner according to claim 2 is characterized in that, described catalytic bed is fixed catalytic bed, and the catalyst carrier of described fixed catalytic bed is graininess, cellular or silk bulk metal or pottery.
4. convection type catalytic burner according to claim 2 is characterized in that, the middle part of cavity or be provided with before the organic exhaust gas import for organic exhaust gas being heated to electrothermal tube or gas-operated thermal bath facility before the urging of predetermined temperature before described urging.
5. convection type catalytic burner according to claim 4 is characterized in that, the bottom of cavity is provided with for detection of thermocouple before the urging of the organic exhaust gas temperature before the contact catalyst before described urging.
6. convection type catalytic burner according to claim 2 is characterized in that, the described height of front cavity of urging is greater than the minor face width of its level cross-sectionn, and the difference of the horizontal sectional area of described horizontal sectional area of urging front cavity and catalytic bed is in preset range.
7. convection type catalytic burner according to claim 6 is characterized in that, described catalytic bed bottom is provided with one and urges rear cavity, and described cleaning exhaust gas outlet is arranged on described bottom of urging rear cavity.
8. convection type catalytic burner according to claim 6, it is characterized in that, described catalytic bed bottom is provided with first and urges cavity, described first urges the side of cavity to be communicated with is provided with second and urges cavity, described second urges the top of cavity to be provided with second catalytic bed of difference in described preset range of horizontal sectional area and catalytic bed horizontal sectional area, the top of described the second catalytic bed is provided with urges rear cavity, and described cleaning exhaust gas outlet is arranged on described top of urging rear cavity.
9. the application of a convection type catalytic burner as claimed in claim 2, it is characterized in that, the cleaning exhaust gas that adopts the cleaning exhaust gas outlet to discharge heats gas or the liquid that need heat, when heating, adopt the cavity type heat exchanger to carry out heat exchange, described cavity type heat exchanger comprises at least one pair of heat exchange cavity, each heat exchanging cavity comprises a heat release cavity and is arranged on the heat absorption cavity on described heat release cavity top, is provided with the heat conduction baffle for heat exchange between described heat release cavity and the heat absorption cavity.
10. the application of convection type catalytic burner according to claim 9, it is characterized in that, when the cavity type heat exchanger comprises many heat exchanging cavity, described many heat exchanging cavity is arranged in order from top to bottom, be provided with the heat conduction baffle for heat exchange between the heat absorption cavity that each heat release cavity is adjacent, described cleaning exhaust gas outlet connects the import of the heat release cavity that is in the top, after cleaning exhaust gas exports the import of the heat release cavity that enters into the top from cleaning exhaust gas, downwards successively by each heat release cavity, discharge from the waste discharge chimney that is communicated with the outlet of the heat release cavity of bottom, the gas that need heat or liquid enter from the import of the heat absorption cavity of bottom, and upwards successively by each heat absorption cavity, being passed into from the outlet of the heat absorption cavity at top needs the destination of using, perhaps when needing heating target to be organic exhaust gas, then directly the outlet of the heat absorption cavity at described top is communicated with organic exhaust gas inlet, to enter into the convection type catalytic burner from described organic exhaust gas import, wherein, the outlet of each heat absorption cavity is arranged on the top of corresponding heat absorption cavity, the outlet of each heat release cavity is arranged on the bottom of corresponding heat release cavity, import and the outlet of each heat absorption cavity, the import of each heat release cavity and the outlet preset distance of all being separated by.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310014050.0A CN103062779B (en) | 2013-01-15 | 2013-01-15 | A kind of convection type catalytic combustion method, burner and application thereof |
| PCT/CN2014/070680 WO2014111019A1 (en) | 2013-01-15 | 2014-01-15 | Convection-type catalytic combustion method, combustor, and heat exchange apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310014050.0A CN103062779B (en) | 2013-01-15 | 2013-01-15 | A kind of convection type catalytic combustion method, burner and application thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103062779A true CN103062779A (en) | 2013-04-24 |
| CN103062779B CN103062779B (en) | 2016-04-27 |
Family
ID=48105534
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310014050.0A Expired - Fee Related CN103062779B (en) | 2013-01-15 | 2013-01-15 | A kind of convection type catalytic combustion method, burner and application thereof |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN103062779B (en) |
| WO (1) | WO2014111019A1 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103471110A (en) * | 2013-09-27 | 2013-12-25 | 天津赛智科技发展有限公司 | Catalytic bed furnace core structure |
| WO2014111019A1 (en) * | 2013-01-15 | 2014-07-24 | Zhou Kaiyong | Convection-type catalytic combustion method, combustor, and heat exchange apparatus |
| CN106247355A (en) * | 2016-09-22 | 2016-12-21 | 北京市环境卫生设计科学研究所 | A kind of high concentration foul gas catalytic oxidation deodorizing equipment and deodorizing method thereof |
| CN107246618A (en) * | 2017-07-26 | 2017-10-13 | 福建省三净环保科技有限公司 | A kind of energy-efficient catalytic combustion device |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB154308A (en) * | 1919-08-21 | 1920-11-22 | Harald Nielsen | Improvements in heat exchange apparatus |
| DE3732655A1 (en) * | 1987-09-28 | 1989-04-13 | Edt Technik Consult Und Umwelt | Heating furnace or water heater for burning solid, liquid or gaseous fuels |
| CN2057220U (en) * | 1988-08-10 | 1990-05-16 | 中国科学院生态环境研究中心 | Purifying and sound eliminating device of exhaust for motor vehicle |
| US5466421A (en) * | 1987-09-21 | 1995-11-14 | Degussa Aktiengesellschaft | Apparatus for the catalytic conversion of waste gases containing hydrocarbon, halogenated hydrocarbon and carbon monoxide |
| US7214351B2 (en) * | 2002-03-29 | 2007-05-08 | Tosoh Corporation | Catalytic combustion reactor with a heat exchanger tube bundle housed therein, catalytic structure and method for carrying out catalytic combustion-reaction using the reactor and the catalytic structure |
| CN201122464Y (en) * | 2007-12-07 | 2008-09-24 | 周开勇 | Energy-saving environment-friendly enamelling machine oven |
| CN202002120U (en) * | 2011-03-25 | 2011-10-05 | 天津赛智科技发展有限公司 | Efficient catalytic combustion purifier for industrial volatilizable organic pollutants |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5184955B2 (en) * | 2008-04-22 | 2013-04-17 | 月島環境エンジニアリング株式会社 | VOC-containing gas processing apparatus and processing method |
| CN202141364U (en) * | 2011-05-06 | 2012-02-08 | 烟台蓝德空调工业有限责任公司 | Sewage box type heat exchanger |
| CN103062779B (en) * | 2013-01-15 | 2016-04-27 | 周开勇 | A kind of convection type catalytic combustion method, burner and application thereof |
-
2013
- 2013-01-15 CN CN201310014050.0A patent/CN103062779B/en not_active Expired - Fee Related
-
2014
- 2014-01-15 WO PCT/CN2014/070680 patent/WO2014111019A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB154308A (en) * | 1919-08-21 | 1920-11-22 | Harald Nielsen | Improvements in heat exchange apparatus |
| US5466421A (en) * | 1987-09-21 | 1995-11-14 | Degussa Aktiengesellschaft | Apparatus for the catalytic conversion of waste gases containing hydrocarbon, halogenated hydrocarbon and carbon monoxide |
| DE3732655A1 (en) * | 1987-09-28 | 1989-04-13 | Edt Technik Consult Und Umwelt | Heating furnace or water heater for burning solid, liquid or gaseous fuels |
| CN2057220U (en) * | 1988-08-10 | 1990-05-16 | 中国科学院生态环境研究中心 | Purifying and sound eliminating device of exhaust for motor vehicle |
| US7214351B2 (en) * | 2002-03-29 | 2007-05-08 | Tosoh Corporation | Catalytic combustion reactor with a heat exchanger tube bundle housed therein, catalytic structure and method for carrying out catalytic combustion-reaction using the reactor and the catalytic structure |
| CN201122464Y (en) * | 2007-12-07 | 2008-09-24 | 周开勇 | Energy-saving environment-friendly enamelling machine oven |
| CN202002120U (en) * | 2011-03-25 | 2011-10-05 | 天津赛智科技发展有限公司 | Efficient catalytic combustion purifier for industrial volatilizable organic pollutants |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014111019A1 (en) * | 2013-01-15 | 2014-07-24 | Zhou Kaiyong | Convection-type catalytic combustion method, combustor, and heat exchange apparatus |
| CN103471110A (en) * | 2013-09-27 | 2013-12-25 | 天津赛智科技发展有限公司 | Catalytic bed furnace core structure |
| CN106247355A (en) * | 2016-09-22 | 2016-12-21 | 北京市环境卫生设计科学研究所 | A kind of high concentration foul gas catalytic oxidation deodorizing equipment and deodorizing method thereof |
| CN107246618A (en) * | 2017-07-26 | 2017-10-13 | 福建省三净环保科技有限公司 | A kind of energy-efficient catalytic combustion device |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2014111019A1 (en) | 2014-07-24 |
| CN103062779B (en) | 2016-04-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102580705B (en) | Comprehensive heat energy utilizing type active coke purifying and regenerating process system and active coke purifying and regenerating process method | |
| CN103062779B (en) | A kind of convection type catalytic combustion method, burner and application thereof | |
| CN101270292B (en) | Cyclic utilization method for tail gas of bituminous shale oil refining | |
| CN111609709A (en) | Two-stage drying and calcining kiln system and method for nitrate-type molded low-temperature denitration catalyst | |
| CN101413398B (en) | Heating start-up system of mine ventilation air methane oxidized apparatus | |
| CN201184696Y (en) | Tube type heating stove | |
| CN102559432B (en) | Energy-saving steaming and boiling system | |
| CN207501170U (en) | Regenerative catalytic combustion device | |
| CN102966978A (en) | Solid and gas multi-fuel water stove | |
| CN109780582B (en) | Liquid methanol heating stove | |
| CN200996720Y (en) | Efficient heater with multiple temperature zone under normal pressure | |
| CN201935600U (en) | Heat exchanger and heat treatment heating system | |
| CN201978636U (en) | Energy-saving efficient adsorption and desorption combined system | |
| CN201636846U (en) | Solid fuel heat-storage type high-temperature air combustion gasification furnace | |
| CN201384925Y (en) | Vertical-type ventilation air methane heat counter-flow oxidization device | |
| CN201508036U (en) | Direct-combustion tube-typed split organic heat carrier boiler | |
| CN201373570Y (en) | Hot-carrier heating furnace | |
| CN210448729U (en) | Scr flue gas denitration system | |
| CN114433021A (en) | Multipurpose resource utilization system and method thereof | |
| CN118031635A (en) | Tubular heating furnace, industrial equipment using tubular heating furnace and heating method | |
| CN112358896A (en) | Biomass gasification Stirling power generation system | |
| CN201837271U (en) | Heat exchanging device and exhaust gas purification system with same | |
| CN101871734A (en) | Heat exchange device and waste gas purification system with same | |
| CN202915555U (en) | High-wind-temperature hot blast stove with high-temperature flue high-temperature flue gas current equalizer | |
| CN206280984U (en) | Regenerative catalytic combustion device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160427 Termination date: 20190115 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |