CN106765217B - A kind of organic waste gas furnace and incinerating method - Google Patents
A kind of organic waste gas furnace and incinerating method Download PDFInfo
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- CN106765217B CN106765217B CN201510802339.8A CN201510802339A CN106765217B CN 106765217 B CN106765217 B CN 106765217B CN 201510802339 A CN201510802339 A CN 201510802339A CN 106765217 B CN106765217 B CN 106765217B
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Abstract
The invention discloses a kind of organic waste gas furnaces, it successively include non-pre-mixing type combustion apapratus according to waste gas flow direction, porous media packing section, 1# heat furnace pipe, catalyst for catalytic oxidation bed and 2# heat furnace pipe, air-vent is set between non-pre-mixing type combustion apapratus and porous media packing section, mixing and burning for organic exhaust gas and fuel, the hot fume generated after burning carries out high-temperature oxydation by porous media packing section, heat after high-temperature oxydation is recycled through 1# heat furnace pipe, catalysis oxidation is carried out subsequently into catalyst bed, exhaust gas is discharged to outside incinerator after 2# heat furnace pipe recycles heat after oxidation.The incinerating method of organic exhaust gas of the present invention is realized by above-mentioned organic waste gas furnace.The present invention improves the efficiency and stability of burning while guaranteeing organic waste-gas purification effect, inherently avoids explosion safety hidden danger caused by organic exhaust gas fluctuation of concentration.
Description
Technical field
The invention belongs to environmentally friendly technical field of waste gas treatment, and in particular to a kind of organic waste gas furnace and incinerating method.
Background technique
Volatile organic waste gas (Volatile Organic Compounds, abbreviation VOCs) is petrochemical enterprise feature
Atmosphere pollution refers to that vapour pressure is greater than or equal under 0.01kPa or specific applicable elements with corresponding at 20 °C
The general designation of volatile organic compound.VOCs is oil refining and petrochemical enterprise characteristic contamination, VOCs master in production process
It will be from process gases, equipment and line component leakage, volatile organic liquid storage and transportation and wastewater collection, processing, storage
The Air Pollutant Emission of facility, can be divided into organized emission source and uncontrollable discharge source, usual uncontrollable discharge amount accounting compared with
Greatly.
It is roughly divided into absorption method, destruction method and direct utilization method for the processing technique of volatile organic waste gas, wherein returning
Receipts method is exactly that the method adsorbed or condensed using the agent of finish absorption and sorption returns most of organic component in organic exhaust gas
Receipts processing, substantially reduces content of organics in exhaust gas, but uses such method treated organic exhaust gas total hydrocarbon content still
It is higher, can not direct qualified discharge, therefore in order to organic exhaust gas carry out deep treatment, it is also necessary to it is carried out using destruction method
It administers, so-called destruction method is exactly to use catalysis oxidation, high-temperature oxydation that organic exhaust gas is carried out deep oxidation processing, and such methods are logical
It often needs using a certain amount of catalyst or builds a hot environment for oxidation operation into carbon dioxide and water, exhaust gas depth
It administers preferably, but its operation and construction cost are higher, when fluctuating biggish object applied to exhaust gas concentration, device operation is steady
It is qualitative poor.And directly utilization method is exactly the directly burning benefit such as the incinerator being passed directly into organic exhaust gas in factory or flare system
Obtain complete burning processing by incinerator with, exhaust gas, reduce VOCs treatment initial investment and day-to-day operation at
This, does not increase treatment facility newly.But organic exhaust gas introducing industrial furnace is had two: first at this stage, the composition of exhaust gas
And flow needs are relatively stable in a certain range, and the fluctuation of exhaust gas is avoided to affect to industry, influence other techniques ginseng
Number fluctuation；Second, the problems such as explosible limit concentration existing for organic exhaust gas, still provides corresponding rule without authoritative institution or unit
Measure is kept away, due to being related to potential security risk, which is not widely approved and used.
CN103697482 discloses a kind of organic exhaust gas boiler heating power burning processing system and treatment process, in boiler air
Balance controller is arranged in machine entrance, the advantage is that: when organic exhaust gas air quantity is unstable, it can be by mending wind at adjustment device
Size keeps the safety and stability of boiler operatiopn, while the air balance controller being arranged is totally-enclosed pipe-line system, Ji Nengwei
The burning air quantity for keeping steady fixed, and exhaust gas leakage problem is not present.But this method blast balance apparatus adjusts air quantity and there is lag
Property, explosion issues of the exhaust gas in explosion limit concentration range are not avoided fundamentally, do not accomplish essential safety.
CN104121591 discloses a kind of energy-efficient incinerator, and this method uses the staggeredly regenerative apparatus being interspersed,
Heat is collected as far as possible and is stored in incinerator, heat is avoided excessively to give out incinerator.In the heat of outflow, by high temperature
On the one hand tail gas is used to heat organic exhaust gas to be burned, on the other hand recycle heat for copper-clad plate production process and to cold
But air preheat.The incinerator structure setting is reasonable, remains 800 DEG C of room temperature of burning or more, low energy consumption, energy
Source utilization rate is high.But the technology does not have still without explosion issues of the exhaust gas in explosion limit concentration range are fundamentally solved
Accomplish essential safety.
CN103759275 discloses a kind of device and method of plasma strengthening multi-hole medium combustion processing organic exhaust gas,
This method acts on Synergistic degradation organic exhaust gas by the accumulation of heat effect of porous media material and plasma free-radical oxidation, improves
The degradation efficiency of organic exhaust gas；The input energy for adjusting plasma according to organic exhaust gas concentration simultaneously is guaranteeing organic waste
Input energy consumption is effectively reduced while gas degradation efficiency.Applied widely with exhaust gas concentration, input energy is low, treatment effeciency
The advantages that height, system controllability and measurability is high.But when organic exhaust gas concentration is higher, there are organic exhaust gas explosion safety problem,
The scope of application of exhaust gas concentration is also than relatively limited.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of organic waste gas furnace and incinerating methods.The present invention exists
While guaranteeing organic waste-gas purification effect, the efficiency and stability of burning are improved, it is dense inherently to avoid organic exhaust gas
Explosion safety hidden danger caused by degree fluctuation.
Organic waste gas furnace provided by the invention successively includes non-pre-mixing type combustion apapratus, porous Jie according to waste gas flow direction
Matter packing section, 1# heat furnace pipe, catalyst for catalytic oxidation bed and 2# heat furnace pipe, non-pre-mixing type combustion apapratus are filled out with porous media
Air-vent is set between material section, for the mixing and burning of organic exhaust gas and fuel, the hot fume generated after burning passes through porous Jie
Matter packing section carries out high-temperature oxydation, and the heat after high-temperature oxydation is recycled through 1# heat furnace pipe, carries out subsequently into catalyst bed
Catalysis oxidation, exhaust gas is discharged to outside incinerator after 2# heat furnace pipe recycles heat after oxidation.
Incinerator of the present invention can be vertical or horizontal cylinder or cube structure, it is preferred to use porous media is filled out
The variable diameter horizontal cylinder structure that material section is relatively large in diameter.Incinerator sectional area keeps the gas flow rate in incinerator in 2-25m/s, excellent
Select 5-15m/s.The distance of the non-pre-mixing type combustion apapratus and porous media packing section is the 2-5 of the burner maximum length of flame
Times, preferably 2-3 times；1# heat furnace pipe is close to 1-3 times that the distance of porous media packing section is porous media filler segment length.It is non-
Pre-mixing type combustion apapratus flame direction, porous media packing section center, 1# heat furnace tube hub, in catalyst for catalytic oxidation bed
The heart, 2# heat furnace tube hub and incinerator export center are on an axis.
Porous media packing section axial length of the present invention is 2-10 times, preferably 3-6 times of diameter.Porous Jie
Matter packing section is sequentially preheating zone, reaction zone and heat-accumulating area, the porous aggregate of the preheating zone along air inlet to gas outlet direction
It is made of porosity and uniform pore diameter or foamed ceramics, the ceramic honey comb etc. that gradually change or be layered variation, aperture is
0.1-10mm, porosity 0.15-0.5；Insulating ceramics, silicon carbide, zirconium oxide or violet can be used in the filler of the reaction zone
Green stone etc., porosity 0.6-0.9；The porous aggregate of the heat-accumulating area can use the filler such as the same specification in preheating zone, or
The scattered heap porous aggregate such as person's porcelain ball.
1# the and 2# heat furnace pipe being arranged before and after catalyst for catalytic oxidation bed of the present invention is that conventional boiler takes heat to change
Hot stove pipe takes heat to cool to one from the flue gas of porous media packing section discharge and from the flue gas that catalyst for catalytic oxidation bed is discharged
Determine temperature, while generating a certain amount of steam, the heat exchange area of heat furnace pipe is adjusted according to exhaust gas temperature.
Catalyst for catalytic oxidation of the present invention uses noble metal catalyst, and carrier is regular carrier or the porcelain balls such as honeycomb type
Etc. scattered heap carrier, precious metals pt, Pd and CeO are supported thereon2Isoreactivity component.
The present invention uses the incinerating method of above-mentioned organic waste gas furnace, through the following steps that realizing safe and stable, high
Effect ground processing organic exhaust gas:
(1) fuel is introduced into the air that incinerator and air-vent enter by non-pre-mixing type combustion apapratus and mixes combining combustion, it will be more
Hole medium filler section temperature is increased to exhaust gas autoignition temperature, then gradually replaces air using organic exhaust gas, and in organic exhaust gas
It is mixed into a certain amount of inert gas before into incinerator, oxygen content in exhaust gas is made to be lower than 8V%；
(2) hot fume after burning carries out high-temperature oxydation by porous media packing section；
(3) exhaust gas after porous media packing section high-temperature oxydation recycles heat through 1# heat furnace pipe；
(4) exhaust gas after recycling heat enters catalyst for catalytic oxidation bed and is aoxidized；
(5) exhaust gas recycles heat, the purified gas discharge of generation or circulating and recovering through 2# heat furnace pipe after aoxidizing.
In the present invention, the fuel of step (1) described burner can be common gaseous fuel and/or liquid fuel, such as
Natural gas, liquefied petroleum gas or fuel oil.Burner is non-pre-mixing type combustion apapratus, i.e. combustion air and fuel is in combustor external
It is mixed and burned, the exhaust gas for entering porous media packing section is preheated, preheating temperature is exhaust gas autoignition temperature.
In the present invention, step (1) the organic exhaust gas total hydrocarbon concentration is less than 60000mg/Nm3, remaining is air, is mixed into one
After quantitative inert gas, dilution oxygen content of waste gas is reduced to 1V%-8V%, while total hydrocarbon concentration being made to be diluted to 23000mg/Nm3With
Under, the total hydrocarbon and oxygen diluted in exhaust gas can guarantee equivalent oxidation reaction.The inert gas can be to be not involved in oxidation instead
The arbitrary gas answered, such as nitrogen, argon gas.
In the present invention, for step (2) after organic exhaust gas is diluted by oxygen content, total hydrocarbon concentration is greater than 8000mg/Nm3When, have
The heat that machine off-gas oxidizing is released can satisfy the maintenance operation certainly of porous media packing section and catalyst for catalytic oxidation bed, and
A certain amount of steam is generated by heat furnace pipe, at this point it is possible to stop the work of burner.When total hydrocarbon concentration is less than 8000mg/
Nm3When, need to fill into a certain amount of fuel by burner to maintain the enough exhaust gas autoignition temperatures of porous media packing section.
In the present invention, step (3) passes through the 1# being arranged between porous media packing section and catalyst for catalytic oxidation bed and takes
Hot stove pipe makes catalyst for catalytic oxidation bed inlet temperatures scope control at 200-450 DEG C, the use of air speed is 10000-
100000h-1.Adjust the use temperature and air speed of catalyst according to the type and concentration of machine object contained in organic exhaust gas, one
Aspect will make organic exhaust gas have preferable clean-up effect, on the other hand organic exhaust gas be avoided to put in catalyst bed reaction again
Heat is more to cause catalyst to inactivate because of high temperature.It is burnt by the way that the control system of the 2# heat furnace after catalyst for catalytic oxidation bed is arranged in
The exhaust gas temperature of burner is at 60-400 DEG C.Oxygen content after organic exhaust gas is mixed with the purified gas (circulating purification gas) of recycling
When greater than 8V% or being less than 1V%, the amount of the organic exhaust gas and circulating purification gas that enter in mixed gas is adjusted, while in order to guarantee
The oxygen content of organic exhaust gas after dilution, fresh inert gas is supplemented into exhaust gas, is made into oxygen in the mixed gas of incinerator
Content is 1 V%-8V%.
In the present invention, purification gas a part that step (5) generates is used as circulating purification gas, is carried out to organic exhaust gas
Mixed diluting, another part purification gas are discharged outside incinerator.
Compared with prior art, the invention has the following advantages:
(1) organic exhaust gas respectively by incinerator burning, porous media high-temperature oxydation, catalyst aoxidize etc. multistage at
Reason, realizes the target of deep treatment, avoids the bad problem of conventional catalyst oxidation catalyst processing lower carbon number hydrocarbons effect.
(2) operating condition operation oxygen content is reduced to explosion limit hereinafter, fundamentally avoiding due to organic exhaust gas by the present invention
Concentration fluctuates widely bring explosion safety hidden danger, substantially increases operation stability and the safety of device.
(3) present invention requires organic exhaust gas concentration more wide in range, can be used according to the organic gas of various concentration from dimension
The mode for holding or being passed through fuel burning operation is handled, and effectively increases the adaptability of device.
(4) part of incineration tail gas utilizes, and carries out mixing preheating to incinerator air inlet, not only saves part energy,
And charge heating also greatly strengthens burning stability.
(5) non-premixed combustion device, porous media packing section, take hot control temperature unit and catalyst for catalytic oxidation bed collection
At substantially reducing plant area and construction cost under the premise of guaranteeing organic exhaust gas deep treatment.
Detailed description of the invention
Fig. 1 is a kind of process flow chart of the method for the present invention；
Wherein: 1- fuel, 2- organic exhaust gas, 3- mixed admission, 4- recycle gaseous mixture, 5- circulating purification gas, 6- indifferent gas
Body, 7- cleaning of off-gas, 8- purified gas, 9- boiler feedwater, 10- steam, 11-1# heat furnace pipe, 12- porous media packing section, 13-
Incinerator, 14- catalyst for catalytic oxidation bed, the non-pre-mixing type combustion apapratus of 15-, 16-2# heat furnace pipe, the preheating zone 17-, 18- are anti-
Answer area, the heat-accumulating area 19-.
Specific embodiment
With reference to the accompanying drawing 1 and embodiment the present invention is furture elucidated method and effect.In the present invention, V% is volume point
Number.
Organic waste gas furnace of the present invention is as shown in Fig. 1, successively include according to waste gas flow direction non-pre-mixing type combustion apapratus 15,
Porous media packing section 12,1# heat furnace pipe 11, catalyst for catalytic oxidation bed 14 and 2# heat furnace pipe 16, wherein porous media
Packing section includes preheating zone 17, reaction zone 18 and heat-accumulating area 19.It is set between non-pre-mixing type combustion apapratus 15 and porous media packing section 12
Air-vent is set, for the mixing and burning of organic exhaust gas 2 and fuel 1, the burning that can also be used as burner provides necessary sky
Gas supplies and as dilution organic exhaust gas import.The hot fume generated after burning carries out high temperature oxygen by porous media packing section 12
Change, the heat after high-temperature oxydation recycles heat through 1# heat furnace pipe 11, carries out catalysis oxidation, warp subsequently into catalyst bed 14
After 2# heat furnace pipe 16 recycles heat, incinerator 13 is discharged in purified gas.
Incinerator 13 of the present invention is vertical or horizontal cylinder structure, and incinerator sectional area is to keep in incinerator 13
Gas flow rate in 5-15m/s.The distance of the non-pre-mixing type combustion apapratus 15 and porous media packing section 12 is that burner is maximum
2-3 times of the length of flame.1# heat furnace pipe 11 is 12 length of porous media packing section close to the distance of porous media packing section 12
1-3 times.15 flame direction of burner, 12 center of porous media packing section, 11 center of 1# heat furnace pipe, catalyst for catalytic oxidation
14 center of bed, 16 center of 2# heat furnace pipe and 13 export center of incinerator are on an axis.
12 axial length of porous media packing section of the present invention is 3-6 times of diameter, along air inlet to gas outlet direction
Be arranged in sequence preheating zone 17, reaction zone 18 and heat-accumulating area 19, the porous aggregate of the preheating zone by porosity and uniform pore diameter or
Person gradually changes or is layered the composition such as foamed ceramics, ceramic honey comb of variation, aperture 0.1-10mm, porosity 0.15-
0.6；Quartz glass, insulating ceramics, silicon carbide, zirconium oxide or cordierite etc., porosity can be used in the filler of the reaction zone
For 0.5-0.9；The porous aggregate of the heat-accumulating area can be more using scattered heaps such as the fillers or porcelain ball of such as same specification in preheating zone
Hole filler.
Heat furnace pipe 11,16 of the invention is that conventional boiler takes heat heat exchange boiler tube, and the heat exchange area of heat furnace pipe is according to row
Smoke temperature degree is adjusted.Catalyst for catalytic oxidation 14 uses noble metal catalyst, and carrier is regular carrier or the porcelain balls such as honeycomb type
Etc. scattered heap carrier, precious metals pt, Pd and CeO are supported thereon2Isoreactivity component.
Using the incinerating method of incinerator as shown in Figure 1, when going into operation, using air as combustion air, by fuel 1 by non-pre-
Mixed burner introduces the air that incinerator 13 and air-vent enter and mixes combining combustion, and 12 temperature of porous media packing section is increased
To exhaust gas autoignition temperature.Then gradually using organic exhaust gas 2 instead of air as burner combustion air, and enter in organic exhaust gas
It is mixed into a certain amount of inert gas 6 before incinerator, makes oxygen content 1V%-8V% in exhaust gas.Hot fume after burning passes through porous Jie
Matter packing section 12 carries out high-temperature oxydation；Exhaust gas after porous media packing section high-temperature oxydation recycles heat through 1# heat furnace pipe 11
It measures, is passed through boiler feedwater 9 in 1# heat furnace pipe 11, steam 10 is generated after exchanging heat.Exhaust gas after recycling heat enters catalysis oxygen
Change catalyst bed 14 to be aoxidized；After oxidation exhaust gas through 2# heat furnace pipe 16 recycle heat after generate purified gas 8 discharge or
Reuse.It generates 8 a part of purified gas to be recycled as circulating purification gas 5, be mixed with inert gas as circulation gaseous mixture 4 one
It rises and mixed diluting is carried out to organic exhaust gas, another part is discharged outside incinerator as cleaning of off-gas 7.
Fuel 1 of the present invention can be common gaseous fuel and liquid fuel, such as natural gas, liquefied petroleum gas or combustion
Material oil, burner 15 are non-pre-mixing type combustion apapratus, i.e. combustion air and fuel is mixed and burned in combustor external, to porous
Medium filler section 12 is preheated, and preheating temperature is 2 autoignition temperature of exhaust gas.2 total hydrocarbon concentration of organic exhaust gas is 50000mg/Nm3,
Remaining is air, and after being mixed into a certain amount of inert gas 6, dilution 3 oxygen content of exhaust gas is reduced to 6V%, while dilutes total hydrocarbon concentration
To 20000mg/Nm3, dilute exhaust gas 3 in total hydrocarbon and oxygen can guarantee equivalent oxidation reaction.The inert gas 6 can be
It is not involved in the arbitrary gas of oxidation reaction, such as nitrogen, argon gas.In the present invention, after organic exhaust gas 2 is diluted by oxygen content, always
Hydrocarbon concentration is greater than 8000mg/Nm3When, the heat that organic exhaust gas oxidation is released can satisfy porous media packing section and catalysis oxidation
Bed generates a certain amount of steam from maintenance operation, and by heat furnace pipe 11,16, at this point it is possible to stop burner 15
Work.When total hydrocarbon concentration is less than 8000mg/Nm3When, it needs to fill into a certain amount of fuel 1 by burner 15 to maintain porous Jie
The enough exhaust gas autoignition temperatures of matter packing section 12.In the present invention, by 1# heat furnace pipe 11, make 14 inlet temperature of catalyst bed
Scope control is 10000-100000h using space velocity range at 200-450 DEG C-1.Incinerator is controlled by 2# heat furnace pipe 16
Exhaust gas temperature is at 60-400 DEG C.When oxygen content is greater than 8V% or is less than 1V% after organic exhaust gas 2 is mixed with circulating purification gas 4, adjust
Section enters the amount of mixed gas organic exhaust gas 2 and circulating purification gas 5, while fresh lazy according to 3 oxygen concentration of gaseous mixture control supplement
Property gas 6 amount, make enter 13 mixed gas of incinerator in oxygen content 1V%-8V%.
Embodiment 1
There are multiple propylene oxide storage tanks in certain chemical company, is equipped with nitrogen protection, and storage tank average exhaust gas discharge amount is 200Nm3/
H, propylene oxide concentrations 138000mg/m3。
It is handled using the incinerator of attached drawing 1, incinerator is horizontal cylinder structure.The holding of incinerator sectional area is burnt
The gas flow rate in furnace is burnt in 15m/s.The distance of the non-pre-mixing type combustion apapratus and porous media packing section is that burner is maximum
3 times of the length of flame；1# heat furnace pipe is close to 3 times that the distance of porous media packing section is porous media filler segment length.It is more
Hole medium filler section axial length is 6 times of diameter, is sequentially preheating zone, reaction zone and accumulation of heat along air inlet to gas outlet direction
The filler in area, the preheating zone is made of the foamed ceramics of porosity and uniform pore diameter, porosity 0.3.The filler of reaction zone
Using silicon carbide, porosity 0.8.The filler of heat-accumulating area uses the porous aggregate such as the same specification in preheating zone.Catalysis oxidation is urged
Agent 14 uses noble metal catalyst, and carrier is honeycomb carrier, supports precious metals pt, Pd and CeO thereon2Active component.
When going into operation, using air as combustion air, natural gas is introduced into the air that incinerator and air-vent enter by non-pre-mixing type combustion apapratus
Mixed combining combustion, is increased to exhaust gas autoignition temperature for porous media packing section temperature.The total hydrocarbon concentration of organic exhaust gas is
138000mg/Nm3, then gradually using organic exhaust gas instead of air as burner combustion air, and enter in organic exhaust gas and burn
It burns stokehold and is mixed into a certain amount of inert nitrogen gas, make oxygen content 3.5V% in exhaust gas, while be diluted to total hydrocarbon concentration
20000mg/Nm3, dilute exhaust gas 3 in total hydrocarbon and oxygen can guarantee equivalent oxidation reaction.Hot fume after burning passes through more
Hole medium filler section 12 carries out high-temperature oxydation, since total hydrocarbon concentration is greater than 8000mg/Nm3When, the heat of organic exhaust gas oxidation releasing
Amount can satisfy the maintenance operation certainly of porous media packing section and catalysis oxidation bed, at this point it is possible to stop the work of burner 15
Make.Exhaust gas after porous media packing section high-temperature oxydation recycles heat through 1# heat furnace pipe, makes catalyst bed inlet temperature
Scope control is 100000h using space velocity range at 450 DEG C-1.Exhaust gas after recycling heat enters catalyst for catalytic oxidation bed
It is aoxidized, exhaust gas recycles heat through 2# heat furnace pipe after oxidation, controls exhaust gas temperature at 200 DEG C.The purified gas of generation is discharged
Or reuse, a part are recycled as circulating purification gas, mix and are used as together with circulation gaseous mixture to organic waste with inert gas
Gas carries out mixed diluting, and another part is discharged outside incinerator as cleaning of off-gas.After organic exhaust gas is mixed with circulating purification gas
When oxygen content is greater than 8V% or is less than 1V%, the amount for entering mixed gas organic exhaust gas and circulating purification gas is adjusted, while according to mixed
The amount that the control of gas oxygen concentration supplements fresh inert gas is closed, makes to enter oxygen content 7V% in incinerator mixed gas.
By above-mentioned processing, purified gas total hydrocarbon concentration≤60mg/Nm of discharge3.Organic exhaust gas passes through burning, regenerative oxidation
Advanced treating has been carried out with catalysis oxidation, has improved the treatment effeciency of organic exhaust gas, simultaneously because oxygen concentration in oxidation process
It is reduced within explosion limit, substantially increases the stability of device operation, avoid security risk to the greatest extent.
Embodiment 2
There are benzene chemical plant installations tail gas, about 500 Nm of tolerance in certain chemical company3/ h, total hydrocarbon concentration are about 53000mg/m3, mainly
Pollutant is benzene, toluene, aniline, cyclohexylamine, hexamethylene etc..
It is handled using the incinerator of attached drawing 1, incinerator is horizontal cylinder structure.The holding of incinerator sectional area is burnt
The gas flow rate in furnace is burnt in 5m/s.The distance of the non-pre-mixing type combustion apapratus and porous media packing section is burner most high fire
2 times of flame length；1# heat furnace pipe is close to 2 times that the distance of porous media packing section is porous media filler segment length.It is porous
Medium filler section axial length is 3 times of diameter, is sequentially preheating zone, reaction zone and accumulation of heat along air inlet to gas outlet direction
The filler in area, preheating zone is made of the foamed ceramics of porosity and uniform pore diameter, porosity 0.15.The filler of reaction zone is removed and is adopted
With cordierite, porosity 0.6.The filler of heat-accumulating area dissipates heap porous aggregate with porcelain ball.Your gold catalyst for catalytic oxidation 14 uses
Metal catalyst, carrier are honeycomb carrier, support precious metals pt, Pd and CeO thereon2Active component.
When going into operation, using air as combustion air, liquefied petroleum gas is introduced into incinerator and air inducing by non-pre-mixing type combustion apapratus
The air that mouth enters mixes combining combustion, and porous media packing section temperature is increased to exhaust gas autoignition temperature.The total hydrocarbon of organic exhaust gas
Concentration is 53000mg/Nm3, then gradually using organic exhaust gas instead of air as burner combustion air, and organic exhaust gas into
It is mixed into a certain amount of inert nitrogen gas before entering incinerator, makes oxygen content 8V% in exhaust gas, while be diluted to total hydrocarbon concentration
20000mg/Nm3, dilute exhaust gas 3 in total hydrocarbon and oxygen can guarantee equivalent oxidation reaction.Hot fume after burning passes through more
Hole medium filler section 12 carries out high-temperature oxydation, since total hydrocarbon concentration is greater than 8000mg/Nm3When, the heat of organic exhaust gas oxidation releasing
Amount can satisfy the maintenance operation certainly of porous media packing section and catalysis oxidation bed, at this point it is possible to stop the work of burner 15
Make.Exhaust gas after porous media packing section high-temperature oxydation recycles heat through 1# heat furnace pipe, makes catalyst bed inlet temperature
Scope control is 10000h using space velocity range at 200 DEG C-1.Exhaust gas after recycling heat enters catalyst for catalytic oxidation bed
It is aoxidized, exhaust gas recycles heat through 2# heat furnace pipe after oxidation, controls exhaust gas temperature at 60 DEG C.The purified gas of generation discharge or
Reuse, a part are recycled as circulating purification gas, mix and are used as together with circulation gaseous mixture to organic exhaust gas with inert gas
Mixed diluting is carried out, another part is discharged outside incinerator as cleaning of off-gas.Oxygen after organic exhaust gas is mixed with circulating purification gas
When content is greater than 8V% or is less than 1V%, the amount for entering mixed gas organic exhaust gas and circulating purification gas is adjusted, while according to mixing
The control of gas oxygen concentration supplements the amount of fresh inert gas, makes to enter oxygen content 8V% in incinerator mixed gas.
By above-mentioned processing, purified gas total hydrocarbon concentration≤60mg/Nm of discharge3.Organic exhaust gas passes through burning, regenerative oxidation
Advanced treating has been carried out with catalysis oxidation, has improved the treatment effeciency of organic exhaust gas, simultaneously because oxygen concentration in oxidation process
It is reduced within explosion limit, substantially increases the stability of device operation, avoid security risk to the greatest extent.
Embodiment 3
There are benzene chemical plant installations tail gas, about 500 Nm of tolerance in certain chemical company3/ h, total hydrocarbon concentration are about 53000mg/m3, mainly
Pollutant is benzene, toluene, aniline, cyclohexylamine, hexamethylene etc..
It is handled using the incinerator of attached drawing 1, incinerator is horizontal cylinder structure.The holding of incinerator sectional area is burnt
The gas flow rate in furnace is burnt in 5m/s.The distance of the non-pre-mixing type combustion apapratus and porous media packing section is burner most high fire
2 times of flame length；1# heat furnace pipe is close to 2 times that the distance of porous media packing section is porous media filler segment length.It is porous
Medium filler section axial length is 3 times of diameter, is sequentially preheating zone, reaction zone and accumulation of heat along air inlet to gas outlet direction
The filler in area, preheating zone is made of the foamed ceramics of porosity and uniform pore diameter, porosity 0.15.The filler of reaction zone is removed and is adopted
With cordierite, porosity 0.6.The filler of heat-accumulating area dissipates heap porous aggregate with porcelain ball.Your gold catalyst for catalytic oxidation 14 uses
Metal catalyst, carrier are honeycomb carrier, support precious metals pt, Pd and CeO thereon2Active component.
When going into operation, using air as combustion air, liquefied petroleum gas is introduced into incinerator and air inducing by non-pre-mixing type combustion apapratus
The air that mouth enters mixes combining combustion, and porous media packing section temperature is increased to exhaust gas autoignition temperature.The total hydrocarbon of organic exhaust gas
Concentration is 53000mg/Nm3, then gradually using organic exhaust gas instead of air as burner combustion air, and organic exhaust gas into
It is mixed into a certain amount of inert nitrogen gas before entering incinerator, makes oxygen content 8V% in exhaust gas, while be diluted to total hydrocarbon concentration
20000mg/Nm3, dilute exhaust gas 3 in total hydrocarbon and oxygen can guarantee equivalent oxidation reaction.Hot fume after burning passes through more
Hole medium filler section 12 carries out high-temperature oxydation, since total hydrocarbon concentration is greater than 8000mg/Nm3When, the heat of organic exhaust gas oxidation releasing
Amount can satisfy the maintenance operation certainly of porous media packing section and catalysis oxidation bed, at this point it is possible to stop the work of burner 15
Make.Exhaust gas after porous media packing section high-temperature oxydation recycles heat through 1# heat furnace pipe, makes catalyst bed inlet temperature
Scope control is 10000h using space velocity range at 200 DEG C-1.Exhaust gas after recycling heat enters catalyst for catalytic oxidation bed
It is aoxidized, exhaust gas recycles heat through 2# heat furnace pipe after oxidation, controls exhaust gas temperature at 60 DEG C.The purified gas of generation discharge or
Reuse, a part are recycled as circulating purification gas, mix and are used as together with circulation gaseous mixture to organic exhaust gas with inert gas
Mixed diluting is carried out, another part is discharged outside incinerator as cleaning of off-gas.Oxygen after organic exhaust gas is mixed with circulating purification gas
When content is greater than 8V% or is less than 1V%, the amount for entering mixed gas organic exhaust gas and circulating purification gas is adjusted, while according to mixing
The control of gas oxygen concentration supplements the amount of fresh inert gas, makes to enter oxygen content 8V% in incinerator mixed gas.
By above-mentioned processing, purified gas total hydrocarbon concentration≤60mg/Nm of discharge3.Organic exhaust gas passes through burning, regenerative oxidation
Advanced treating has been carried out with catalysis oxidation, has improved the treatment effeciency of organic exhaust gas, simultaneously because oxygen concentration in oxidation process
It is reduced within explosion limit, substantially increases the stability of device operation, avoid security risk to the greatest extent.
Comparative example 1
Processing unit and operating process with embodiment 1, the difference is that: porous media packing section setting be all by hole
The foamed ceramics of rate and uniform pore diameter composition, porosity 0.15.Entire incinerator pressure drop greatly increases, to increase entire
The operating power consumption of device.
Comparative example 2
Processing unit and operating process with embodiment 1, the difference is that: porous media packing section setting be all by hole
The silicon carbide of rate and uniform pore diameter composition, porosity 0.8.Heat storage efficiency reduces, and reaction zone temperature reduces, and organic matter is reacting
The oxidation efficiency in area reduces.
Claims (12)
1. a kind of incinerating method of organic exhaust gas, it is characterised in that be to be realized using following incinerator, the incinerator according to
Waste gas flow direction successively include non-pre-mixing type combustion apapratus, porous media packing section, 1# heat furnace pipe, catalyst for catalytic oxidation bed and
Air-vent is arranged between the non-pre-mixing type combustion apapratus and the porous media packing section in 2# heat furnace pipe；Specifically include following step
It is rapid:
(1) fuel is introduced into the air that incinerator and air-vent enter by non-pre-mixing type combustion apapratus and mixes combining combustion, by porous Jie
Matter packing section temperature is increased to exhaust gas autoignition temperature, then gradually replaces air using organic exhaust gas, and enter in organic exhaust gas
It is mixed into a certain amount of inert gas before incinerator, oxygen content in exhaust gas is made to be lower than 8V%；
(2) hot fume after burning carries out high-temperature oxydation by porous media packing section；
(3) exhaust gas after porous media packing section high-temperature oxydation recycles heat through 1# heat furnace pipe；
(4) exhaust gas after recycling heat enters catalyst for catalytic oxidation bed and is aoxidized；
(5) exhaust gas recycles heat, the purified gas discharge of generation or circulating and recovering through 2# heat furnace pipe after aoxidizing.
2. incinerating method according to claim 1, it is characterised in that: the incinerator is vertical or horizontal cylinder or vertical
Cube structure, incinerator sectional area are to keep the gas flow rate in incinerator in 2-25m/s.
3. incinerating method according to claim 1, it is characterised in that: the non-pre-mixing type combustion apapratus and porous media filler
The distance of section is 2-5 times of the burner maximum length of flame, and 1# heat furnace pipe is porous close to the distance of porous media packing section
1-3 times of medium filler segment length.
4. incinerating method according to claim 1, it is characterised in that: non-pre-mixing type combustion apapratus flame direction, porous media
In packing section center, 1# heat furnace tube hub, catalyst for catalytic oxidation bed center, 2# heat furnace tube hub and burning outlet of still
The heart is on an axis.
5. incinerating method according to claim 1, it is characterised in that: the porous media packing section axial length is diameter
2-10 times, the porous media packing section is sequentially preheating zone, reaction zone and heat-accumulating area along air inlet to gas outlet direction；
The porous aggregate of the preheating zone is by porosity and uniform pore diameter or gradually changes or be layered the foamed ceramics changed or bee
Nest ceramics composition, aperture 0.1-10mm, porosity 0.15-0.5；The filler of the reaction zone uses insulating ceramics, carbonization
Silicon, zirconium oxide or cordierite, porosity 0.6-0.9；The porous aggregate of the heat-accumulating area is filled out using the same specification in preheating zone
The scattered heap porous aggregate such as material or porcelain ball.
6. incinerating method according to claim 1, it is characterised in that: the catalyst for catalytic oxidation uses precious metal catalyst
Agent, carrier are that the regular carrier of honeycomb type or porcelain ball dissipate heap carrier, support precious metals pt, Pd and CeO thereon2Active component.
7. incinerating method according to claim 1, it is characterised in that: the fuel of step (1) described burner can be gas
Fluid fuel and/or liquid fuel, burner are non-pre-mixing type combustion apapratus, i.e. combustion air and fuel is mixed in combustor external
Combination burning preheats the exhaust gas for entering porous media packing section, and preheating temperature is exhaust gas autoignition temperature.
8. incinerating method according to claim 1, it is characterised in that: step (1) the organic exhaust gas total hydrocarbon concentration is less than
60000mg/Nm3, remaining is air, and after being mixed into a certain amount of inert gas, dilution oxygen content of waste gas is reduced to 1V%-8V%, simultaneously
Total hydrocarbon concentration is set to be diluted to 23000mg/Nm3Hereinafter, the total hydrocarbon and oxygen in dilution exhaust gas can guarantee equivalent oxidation reaction.
9. incinerating method according to claim 1, it is characterised in that: step (2) when organic exhaust gas by oxygen content dilute after,
Total hydrocarbon concentration is greater than 8000mg/Nm3When, the heat that organic exhaust gas oxidation is released can satisfy porous media packing section and catalysis oxygen
That changes catalyst bed generates a certain amount of steam from maintenance operation, and by heat furnace pipe, stops the work of burner at this time；
When total hydrocarbon concentration is less than 8000mg/Nm3When, a certain amount of fuel is filled by burner to maintain porous media packing section enough
Exhaust gas autoignition temperature.
10. incinerating method according to claim 1, it is characterised in that: step (3) is by being arranged in porous media packing section
1# heat furnace pipe between catalyst for catalytic oxidation bed, makes catalyst for catalytic oxidation bed inlet temperatures scope control in 200-
450 DEG C, be 10000-100000h using air speed-1；By the way that the control system of the 2# heat furnace after catalyst for catalytic oxidation bed is arranged in
The exhaust gas temperature of incinerator is at 60-400 DEG C.
11. incinerating method according to claim 1, it is characterised in that: when organic exhaust gas and the purified gas of recycling are mixed
When oxygen content is greater than 8V% or is less than 1V% after conjunction, the amount of the organic exhaust gas and circulating purification gas that enter in mixed gas is adjusted, to
Fresh inert gas is supplemented in exhaust gas, is made into 1 V%-8V% of oxygen content in the mixed gas of incinerator.
12. incinerating method according to claim 1, it is characterised in that: a part of conduct of purification gas that step (5) generates
Circulating purification gas uses, and carries out mixed diluting to organic exhaust gas, another part purification gas is discharged outside incinerator.
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