CN206881511U - A kind of safety-type catalysis oxidation VOCs of temperature control administers reactor - Google Patents
A kind of safety-type catalysis oxidation VOCs of temperature control administers reactor Download PDFInfo
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- CN206881511U CN206881511U CN201720752645.XU CN201720752645U CN206881511U CN 206881511 U CN206881511 U CN 206881511U CN 201720752645 U CN201720752645 U CN 201720752645U CN 206881511 U CN206881511 U CN 206881511U
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Abstract
The utility model discloses a kind of safety-type catalysis oxidation VOCs of temperature control to administer reactor, including catalytic reactor, gas access is provided with the top of the catalytic reactor, bottom is provided with gas vent, longitudinal arrangement has reactor tubulation in the catalytic reactor, the upper and lower ends of the reactor tubulation are fixed on dividing plate and stretch out dividing plate, and sealing cavity is formed between the catalytic reactor, reactor tubulation and dividing plate, recyclable conduction oil is filled with the sealing cavity；The catalytic reactor top is provided with conduction oil outlet, and bottom is provided with heat conduction oil-in；Upper strata is filled with stainless steel cloth or porcelain ball inside the reactor tubulation, middle level is filled with catalyst, lower floor is filled with heat conduction and support porcelain ball, reactor heat storage capacity disclosed in the utility model is powerful, reaction temperature is precisely controllable, safe and reliable, is particularly suitable for handling big flow, the situation of interval material air inlet.
Description
Technical field
It the utility model is related to volatile organic matter (VOCs) and administer field, more particularly to a kind of heat storage capacity is powerful, anti-
Answer the improvement reactor of accurate controllable, the safe and reliable efficient process VOCs tail gas of temperature.
Background technology
Catalysis oxidation VOCs treatment technologies are generally used for handling the VOCs materials of low concentration, recently as country and place
Environmental protection standard upgrades, and VOCs emission limits are increasingly strict.When traditional VOCs Treatment process can not be long such as absorption method, condensation method
Between, high efficiency processing low concentration VOCs materials, and the VOCs materials of this low concentration generally pass through catalysis oxidation VOCs administer end
End technology is destroyed, so as to meet environmental protection index requirement.
In existing low-temperature catalytic oxidation technology handle low concentration VOCs materials when be to be changed first by heat exchanger
Heat heating VOCs materials, the mode for being warming up to the temperature needed for reactor reaction, VOCs are directly heated secondly by electric heater
Material is stepped up VOCs material tolerance after reaching preheating temperature, and it is finally reached reaction condition.Initial reaction prepares
Time is grown, and efficiency is low, and has the following disadvantages：
1) reactor temperature change is closely related with VOCs material concentrations, and VOCs material concentrations are higher, and reactor is in itself
The heat of release is bigger, lacks necessary temperature adjustment means.
2) reactor lacks effective heat storage capacity in itself, and the heat that reactor discharges in itself can not be preserved effectively；Often
It is weaker to advise reactor heat storage capacity, thermal storage ceramic is normally filled with reactor and carries out accumulation of heat, thermal storage ceramic is generally only once
Heat storage capacity, thermal storage time length, radiating time are fast, it is impossible to effective meet demand.
3) traditional reactor is due to lacking indispensable temperature adjustment measure, and reactor design temperature is higher, and equipment bears thermal stress
Greatly, the cost of manufacture of equipment is added.
Utility model content
In order to solve the above technical problems, the utility model, which provides a kind of safety-type catalysis oxidation VOCs of temperature control, administers reaction
Device, to reach raising heat storage capacity, energy-saving effect is improved, improves the purpose of security of system.
To reach above-mentioned purpose, the technical solution of the utility model is as follows：
A kind of safety-type catalysis oxidation VOCs of temperature control administers reactor, including catalytic reactor, the catalytic reactor top
Portion is provided with gas access, and bottom is provided with gas vent, and longitudinal arrangement has reactor tubulation, the reaction in the catalytic reactor
The upper and lower ends of device tubulation are fixed on dividing plate and stretch out dividing plate, between the catalytic reactor, reactor tubulation and dividing plate
Sealing cavity is formed, recyclable conduction oil is filled with the sealing cavity；The catalytic reactor top is provided with conduction oil
Outlet, bottom is provided with heat conduction oil-in；Upper strata is filled with stainless steel cloth or porcelain ball inside the reactor tubulation, and middle level loads
There is catalyst, lower floor is filled with heat conduction and support porcelain ball.
In such scheme, the sealing cavity top is provided with conduction oil upper thermocouple, and bottom is provided with conduction oil bottom heat
Galvanic couple, for monitoring the temperature of conduction oil.
In such scheme, the reactor tubulation top is provided with upper strata thermocouple in tubulation, and bottom is provided with lower floor in tubulation
Thermocouple, for monitoring the temperature of gas in tubulation.
In such scheme, the opening position in the catalytic reactor positioned at gas access is distributed provided with hemispheric gas
Device, the radian of gas distributor and the end socket radian of catalytic reactor match, while are provided with gas distributor some equal
The through hole of even distribution, mixed gas are mainly entered in reactor tubulation by through hole.
In further technical scheme, heat transmission fin is evenly distributed with outside the reactor tubulation, further lifting heat exchange
Effect.
Annular or circular deflection plate is provided with further technical scheme, in the sealing cavity.
Pass through above-mentioned technical proposal, the safety-type catalysis oxidation VOCs of temperature control provided by the utility model administer reactor with showing
The beneficial effect for having technology to compare is：
1) heat storage capacity is strong, VOCs air inlets material interval air inlet or flowed fluctuation scope be big or material concentration excursion
With the obvious advantage in the case of big, VOCs air inlet materials still are able to react with high efficiency, so as to promote VOCs good purifications.
2) system is safe and reliable, avoids VOCs air inlets material from directly being contacted with electric heater high temperature electric heating tube, heat conduction thing
Material temperature degree more controllable precise；Avoid producing electric spark because electric heater electrical leakage or electric heating tube interior insulation ability fail and causing
The dangerous generation of oil gas explosion；
3) energy-saving effect is notable, and it is notable to reduce electrical equipment stop frequency, the energy-saving effects such as electric heater.
4) power load reduces, and after heat storage capacity lifting, power load greatly reduces.
Brief description of the drawings
, below will be to embodiment in order to illustrate more clearly of the utility model embodiment or technical scheme of the prior art
Or the required accompanying drawing used is briefly described in description of the prior art.
Fig. 1 is a kind of knot of the safety-type catalysis oxidation VOCs improvement reactor of temperature control disclosed in the utility model embodiment
Structure schematic diagram；
Fig. 2 is the reactor tubulation schematic diagram disclosed in the utility model embodiment；
Fig. 3 is the application system of the safety-type catalysis oxidation VOCs improvement reactor of temperature control disclosed in the utility model embodiment
System schematic diagram.
In figure, 1, master air suction valve door；2nd, control valve is diluted；3rd, blower fan；4th, catalytic reactor；41st, gas access；42、
Gas distributor；43rd, reactor tubulation；431st, stainless steel cloth or porcelain ball；432nd, catalyst；433rd, heat conduction and support porcelain ball；
434th, heat transmission fin；44th, gas reactor exports；45th, heat conduction oil-in；46th, conduction oil outlet；471st, conduction oil top thermoelectricity
It is even；472nd, upper strata thermocouple in tubulation；473rd, lower floor's thermocouple in tubulation；474th, conduction oil bottom thermocouple；48th, dividing plate；49、
Deflection plate；5th, chimney；6th, electric heater；7th, Heat-transfer Oil Pump；8th, gs-oil separator；9th, expansion slot；10th, condenser.
Embodiment
Below in conjunction with the accompanying drawing in the utility model embodiment, the technical scheme in the embodiment of the utility model is carried out
Clearly and completely describe.
The utility model provides a kind of safety-type catalysis oxidation VOCs of temperature control and administers reactor, structure as shown in Figure 1,
On the premise of heat exchange efficiency does not reduce, heat storage capacity is obviously improved the catalytic reactor, and conduction oil can be heated storage in advance
Heat energy.Changes in flow rate is especially handled greatly or in the case of interval air inlet, is made in the presence of the oil stream amount that can be exchanged heat by regulation
It meets duty requirements；So as to reduce system time, improve plant running and handle VOCs efficiency；And it is particularly suitable for locating
Manage the situation of the air inlet of interval material and big flow VOCs air inlets.
The safety-type catalysis oxidation VOCs of temperature control as shown in Figure 1 administers reactor, including catalytic reactor 4, catalytic reaction
The top of device 4 is provided with gas access 41, and bottom is provided with gas vent 44, and longitudinal arrangement has reactor tubulation 43 in catalytic reactor 4,
The upper and lower ends of reactor tubulation 43 are fixed on dividing plate 48 and stretch out dividing plate 48, catalytic reactor 4, reactor tubulation 43 and
Sealing cavity is formed between dividing plate 48, recyclable conduction oil is filled with sealing cavity；The top of catalytic reactor 4 is provided with heat conduction
Oil export 46, bottom are provided with heat conduction oil-in 45；As shown in Fig. 2 the inside upper strata of reactor tubulation 43 is filled with stainless steel cloth
Or porcelain ball 431, middle level are filled with catalyst 432, lower floor is filled with heat conduction and support porcelain ball 433.
Sealing cavity top is provided with conduction oil upper thermocouple 471, and bottom is provided with conduction oil bottom thermocouple 474, is used for
Monitor the temperature of conduction oil.The top of reactor tubulation 43 is provided with upper strata thermocouple 472 in tubulation, and bottom is provided with lower floor's heat in tubulation
Galvanic couple 473, for monitoring the temperature of gas in reactor tubulation 43.
Technical solutions of the utility model are specific as follows：
VOCs materials deliver to main air inlet pipe road through blower fan 3 after being mixed with diluent gas and enter catalytic reaction from gas access 41
In device 4, mixed material enters in catalytic reactor 4 walks tube side into reactor tubulation 43.Upper strata is stainless in reactor tubulation 43
Steel wire or porcelain ball 431, which are used to exchange heat, to heat up, and reaches the initial reaction temperature of catalytic reaction；The bed of middle level catalyst 432 is used for
Generation catalytic reaction, VOCs materials are converted into carbon dioxide and vapor in this layer, and discharge heat；Bottom heat conduction and support porcelain
433 layers of ball is used to cool and support.High efficient heat exchanging heat conduction high-temp liquid heat conduction is filled with the shell side sealing cavity of catalytic reactor 4
Oil；Mixed material reaches reaction temperature through the heating that exchanges heat on tube side upper strata and is converted into two in the presence of the catalyst of tube side middle level
Carbonoxide and vapor simultaneously discharge heat；Cool when flowing through tube side lower floor porcelain spherical space with adopting heat transfer liquid for heat exchange in shell side, most
The mixed material after purification is discharged from gas vent 44 eventually.
Designing points：
1) the entry and exit pipe diameter determing of catalytic reactor 4, it is first determined 4 maximum inlet flow rate of catalytic reactor, typically take
10-15m/s, secondly it is determined that on the premise of maximum reaction flow, maximum reaction flow calculates with air inlet caliber velocity ratio
Catalytic reactor gateway caliber；
2) according to full admission amount and catalyst self character, catalyst institute expense is calculated, air speed is typically designed and takes
2000-3000m3/(m3·h)；Catalyst diameter typically takes 3-5mm；Consider that wall effect tubulation diameter typically takes spherical simultaneously
8-12 times of grain diameter；For the balanced resistance drop of different reactor tubulation 43, the 10 of catalyst reaction bed length ≮ tubulation diameter
Times；
3) catalyst upper strata loads stainless steel cloth or porcelain ball isodiametric with catalyst composition, upper strata in reactor tubulation
Stainless steel cloth or porcelain ball height are calculated according to heat exchange area and determined；
4) it is chilling area that catalyst lower floor, which is equally filled with the isodiametric porcelain ball of catalyst, lower floor, in reactor tubulation,
Porcelain ball bed height determines according to heat exchange cooling areal calculation；
5) heat transmission fin has been evenly arranged outside reactor tubulation, for improving heat transfer effect；
6) between conduction oil operating temperature is 300-330 DEG C, tubulation highest focus design load is 450 DEG C in reactor；
7) opening position in catalytic reactor 4 positioned at gas access is provided with hemispheric gas distributor 42, gas distribution
The end socket radian of the radian of device 42 and catalytic reactor 4 matches, while some be uniformly distributed is provided with gas distributor 42
Through hole, mixed gas mainly by through hole enter reactor tubulation 43 in.The arrangement form of such a gas distributor 42 is easy to
Air-flow branch, in preferable Flat push air-flow；
8) annular or circular deflection plate 49 is provided with the sealing cavity shell side of catalytic reactor 4.
The application system schematic diagram of the catalytic reactor 4 as shown in Figure 3, the gas access of catalytic reactor 4 passes through pipe
Road connection master air suction valve door 1, dilution control valve 2 and blower fan 3, gas vent 44 connect chimney 5 by pipeline.Heat conduction oil-in
Heat-conduction oil circulation system is connected between 45 and conduction oil outlet 46, the Heat-conduction oil circulation system includes passing through with heat conduction oil-in 45
The Heat-transfer Oil Pump 7 and electric heater 6 of pipeline connection, Heat-transfer Oil Pump 7 connect conduction oil by gs-oil separator 8 and condenser 10 and gone out
Mouth 46, gs-oil separator 8 connect expansion slot 9 outside.
Before the non-commencement of commercial operation of system, Heat-conduction oil circulation system starts first.After Heat-transfer Oil Pump 7 starts, electric heater 6
Run and form oil circulation between catalytic reactor 4, gs-oil separator 8, Heat-transfer Oil Pump 7 and electric heater 6.Conduction oil by
Heat conduction oil-in 45 enters the shell side of catalytic reactor 4, enters gs-oil separator 8 by conduction oil outlet 46 afterwards.With oil temperature
Rise, entered after gas hot expanding type by gs-oil separator 8 in expansion slot 9 and stored.Heat conduction oil temperature can pass through catalytic reactor 4
Conduction oil upper thermocouple 471 and conduction oil bottom thermocouple 474 in shell side monitor in real time.On electric heater 6 and conduction oil
PID is adjusted between portion's thermocouple 471 and conduction oil bottom thermocouple 474.Treat conduction oil upper thermocouple 471 and conduction oil bottom
After thermocouple 474 reaches operating temperature needed for system, electric heater and Heat-transfer Oil Pump are stopped.Heat-conduction oil circulation system makes
With electric heater capacity can greatly be reduced, major part " heat energy " is set to be stored in conduction oil, it is full so as to realize heat accumulation function
The situation of sufficient interval material air inlet or big flow air inlet once in a while.
System is the reaction condition for possessing processing VOCs.Now master air suction valve 1 is opened, and dilution regulating valve 2 is opened, blower fan
3 start.Mixed material is entered in catalytic reaction by gas access 41.It is and real by the gas distributor 42 of catalytic reactor 4
The existing radially uniform branch of gas, into the tube side of reactor tubulation 43.
In a kind of preferred embodiment, catalyst main active is noble metal, and is supported on Alumina spheres, instead
Answer the tube side orlop of device tubulation 43 arrangement porcelain ball 433；Catalyst 432 is arranged in tubulation tube side middle level, and catalyst diameter isBetween, 10 times of a diameter of catalyst pellets particle diameter of tube side, reaction bed length ≮ tube side in reactor
10 times of diameter；The reactor tubulation tube side the superiors arrange stainless steel cloth.It is stainless that mixed gas enters reactor tubulation tube side
Steel screen layer is exchanged heat with out-of-bounds conduction oil, and mixed gas heating reaches initial reaction temperature, reactor upper strata heat conduction oil temperature
Degree reduces.Mixed gas enters tubulation tube side middle level, is reacted in the presence of the catalyst of middle level and discharges heat, conduction oil
Temperature raises after absorbing heat.Due to the effect of the temperature difference, conduction oil forms thermal convection current in reactor.If conduction oil itself heat is right
In the case that stream effect is relatively low, the circulation of conduction oil is realized using outside conduction oil circulation power Heat-transfer Oil Pump 7.VOCs itself is anti-
The heat that should be discharged can preferably be absorbed by conduction oil and be transferred to upper strata and continue to be absorbed by new mixing gas at normal temperature, from
And maintain thermal balance.Simultaneously in order to increase heat exchange efficiency, fin 434 is installed outside reactor tubulation 43, so as to further carry
Heat transfer effect is risen.
When the situation of interval air inlet occurs, because conduction oil heat storage capacity is extremely strong, heat loss is minimum, so as to promote
Heat conduction oil temperature is maintained in reasonable working range in reactor shell side.The heat conduction oil temperature in the case of long period not air inlet
When declining, lost by fine start Heat-transfer Oil Pump 7 and the additional heat of electric heater 6.So that it is guaranteed that system can be located all the time
In stand-by operation state, therefore it is particularly suitable for handling the situation of interval material air inlet.
In the case where flow has great fluctuation process, by increasing startup and changing the ability to work of Heat-transfer Oil Pump 7, make its satisfaction
The demand of gas with various flow.
The foregoing description of the disclosed embodiments, professional and technical personnel in the field are enable to realize or new using this practicality
Type.A variety of modifications to these embodiments will be apparent for those skilled in the art, determine herein
The General Principle of justice can be realized in other embodiments in the case where not departing from spirit or scope of the present utility model.Cause
This, the utility model is not intended to be limited to the embodiments shown herein, and is to fit to and principles disclosed herein
The most wide scope consistent with features of novelty.
Claims (6)
1. a kind of safety-type catalysis oxidation VOCs of temperature control administers reactor, including catalytic reactor, the catalytic reactor top
Provided with gas access, bottom is provided with gas vent, it is characterised in that longitudinal arrangement has reactor row in the catalytic reactor
Pipe, the upper and lower ends of the reactor tubulation are fixed on dividing plate and stretch out dividing plate, the catalytic reactor, reactor tubulation with
And sealing cavity is formed between dividing plate, filled with recyclable conduction oil in the sealing cavity；The catalytic reactor top
Provided with conduction oil outlet, bottom is provided with heat conduction oil-in；Upper strata is filled with stainless steel cloth or porcelain inside the reactor tubulation
Ball, middle level are filled with catalyst, and lower floor is filled with heat conduction and support porcelain ball.
2. the safety-type catalysis oxidation VOCs of a kind of temperature control according to claim 1 administers reactor, it is characterised in that described
Sealing cavity top is provided with conduction oil upper thermocouple, and bottom is provided with conduction oil bottom thermocouple.
3. the safety-type catalysis oxidation VOCs of a kind of temperature control according to claim 1 administers reactor, it is characterised in that described
Reactor tubulation top is provided with upper strata thermocouple in tubulation, and bottom is provided with lower floor's thermocouple in tubulation.
4. the safety-type catalysis oxidation VOCs of a kind of temperature control according to claim 1 administers reactor, it is characterised in that described
Opening position in catalytic reactor positioned at gas access is provided with hemispheric gas distributor.
5. administering reactor according to a kind of any safety-type catalysis oxidation VOCs of described temperature control of claim 1 or 3, its feature exists
In the reactor tubulation is evenly distributed with heat transmission fin outside.
6. administering reactor according to a kind of any safety-type catalysis oxidation VOCs of described temperature control of claim 1 or 2, its feature exists
In provided with annular or circular deflection plate in the sealing cavity.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720752645.XU CN206881511U (en) | 2017-06-27 | 2017-06-27 | A kind of safety-type catalysis oxidation VOCs of temperature control administers reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720752645.XU CN206881511U (en) | 2017-06-27 | 2017-06-27 | A kind of safety-type catalysis oxidation VOCs of temperature control administers reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108543500A (en) * | 2018-06-28 | 2018-09-18 | 钦州学院 | The pipeline catalyst reaction device of liquid phase |
| CN109126454A (en) * | 2017-06-27 | 2019-01-04 | 中国石油化工股份有限公司 | A kind of safety-type catalysis oxidation VOCs improvement reactor of temperature control |
-
2017
- 2017-06-27 CN CN201720752645.XU patent/CN206881511U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109126454A (en) * | 2017-06-27 | 2019-01-04 | 中国石油化工股份有限公司 | A kind of safety-type catalysis oxidation VOCs improvement reactor of temperature control |
| CN108543500A (en) * | 2018-06-28 | 2018-09-18 | 钦州学院 | The pipeline catalyst reaction device of liquid phase |
| CN108543500B (en) * | 2018-06-28 | 2024-02-13 | 钦州学院 | Pipeline catalytic reaction device for liquid phase |
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