CN212167011U - Equipment for treating VOCs gas by using flue gas - Google Patents
Equipment for treating VOCs gas by using flue gas Download PDFInfo
- Publication number
- CN212167011U CN212167011U CN202020589234.5U CN202020589234U CN212167011U CN 212167011 U CN212167011 U CN 212167011U CN 202020589234 U CN202020589234 U CN 202020589234U CN 212167011 U CN212167011 U CN 212167011U
- Authority
- CN
- China
- Prior art keywords
- flue gas
- reaction tank
- gas
- incinerator
- cupola
- 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.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model provides an utilize gaseous equipment of flue gas treatment VOCs, equipment includes: the pre-reaction tank is used for the intermixing reaction of the flue gas of the cupola furnace and the flue gas of the incinerator; a gas catcher for further catching of flue gas; the desulfurization reaction tank is used for the intermixing reaction of a desulfurizing agent and flue gas; a desulfurizer spraying device is arranged at the top of the desulfurization reaction tank; the pre-reaction tank, the gas catcher and the desulfurization reaction tank are sequentially connected. The utility model discloses an equipment structure that VOCs is gaseous is handled to flue gas is simple, and the cost is low, and area is little, can realize the gaseous high-efficient innocent treatment of VOCs through this equipment, and the result of formation only needs simple solid useless processing, need not to introduce too much treatment facility, green.
Description
Technical Field
The utility model relates to a flue gas treatment field of insulation material trade particularly, relates to an utilize flue gas to handle gaseous equipment of VOCs.
Background
The flue gas emission of the thermal insulation material industry mainly comprises two parts: the flue gas chemical components of the two parts are different, and the components of the flue gas of the cupola furnace for melting the ores mainly comprise smoke dust particles, sulfur dioxide and nitrogen oxides. The main chemical components of the incinerator flue gas of the thermal insulation material curing production line and the cotton collecting production line are formaldehyde, phenol and methane total hydrocarbons (VOCs).
In the prior art, the cupola flue gas treatment mainly adopts a cloth bag dust removal method, a desulfurizing tower method, an SCRS method and an NCR method. The main treatment method of the incinerator flue gas comprises the following steps: 1. condensation recovery method: VOCs produced in the industry are directly introduced into a condenser, and waste gas reaches the emission standard through the actions and reactions of links such as adsorption, absorption, analysis, separation and the like. 2. Physical absorption method: the waste gas is introduced into absorption liquid for absorption and purification, and the absorption liquid is saturated and then is subjected to treatment such as heating, analysis, condensation and the like. 3. The direct combustion method comprises the following steps: the waste gas is ignited by using auxiliary materials such as fuel gas and the like, so that harmful substances in the waste gas are promoted to be converted into harmless substances under the high-temperature combustion. 4. A catalytic combustion method: the waste gas is heated and converted into harmless carbon dioxide and water after catalytic combustion. 5. An adsorption method: the organic waste gas is adsorbed and purified by using active carbon. High investment, high energy consumption, large equipment volume and long construction period.
Therefore, the treatment methods have the problems of high energy consumption, high investment, high treatment difficulty, high operation cost and the like.
In view of this, the present invention is especially provided.
SUMMERY OF THE UTILITY MODEL
A first object of the present invention is to provide a method for treating VOCs with flue gas, which comprises mixing flue gas from cupola and incinerator for reactionSO in cupola flue gas2、NOXHCHO and C in the smoke of the incinerator and the same components6H5-OH、CH4The components are reacted, and pollution-free products are respectively generated after the reaction is completed, the treatment method simultaneously achieves scientific treatment on VOCs gas and toxic gas containing nitrogen and sulfur, the method is low in operation cost, simple and convenient to operate, good in treatment effect, and capable of generating products with high added values for recycling.
A second object of the utility model is to provide an adopt above-mentioned treatment facility of processing method, this equipment structure is simple, and the cost is low, and area is little, can realize the gaseous high-efficient innocent treatment of VOCs through this equipment, and the result of formation only needs simple solid useless processing, need not to introduce too much treatment facility, green.
In order to realize the above purpose of the utility model, the following technical scheme is adopted:
the utility model provides a method for treating VOCs gas by using flue gas, comprising the following steps:
the flue gas of the cupola furnace and the flue gas of the incinerator are mixed in a proportion of 1: (1.8-3), adding a desulfurizing agent after the reaction, and continuing the reaction, wherein the desulfurizing agent is preferably inorganic base.
In the prior art, the flue gas of the cupola furnace and the flue gas of the incinerator are treated in a harmless way respectively, but the problems of high treatment cost, high treatment difficulty, incomplete treatment and the like exist.
The utility model discloses a solve above-mentioned technical problem, utilized two kinds of flue gas compositions mixable to carry out the characteristics of chemical reaction, can realize simultaneously to the disposable processing of two kinds of flue gases like this, not only reduced the processing operation degree of difficulty, greatly reduced treatment cost moreover to in order to satisfy two kinds of flue gases fully react, handle thorough effect, the volume ratio of two kinds of flue gases has also carried out a large amount of practices and has sargent, discovery cupola flue gas with burn burning furnace flue gas and need be with volume ratio 1: (1.8-3), preferably the volume ratio of the flue gas of the cupola furnace to the flue gas of the incinerator is 1 (1.9-2.5), more preferably 1:2.
In addition, the volume ratio of the cupola flue gas to the incinerator flue gas can be 1:2.2, 1:2.3, 1:2.4, 1:2.6, 1:2.7, 1:2.8, 1:2.9 and the like.
Preferably, as a further implementable scheme, the desulfurizing agent is at least one of sodium hydroxide, potassium hydroxide and magnesium hydroxide, preferably sodium hydroxide, the sodium hydroxide is cheap and easily available, and the desulfurizing effect is good.
Preferably, as a further practicable scheme, the flow rates of the cupola flue gas and the incinerator flue gas are controlled to be between 1 and 15m/s, preferably between 3 and 7.5m/s, and the flow rates of the two flue gases are sufficiently reduced, so that the two flue gases can be mixed and reacted more completely. In actual operation, different flow rates can be adopted in different reaction stages, so that the flow rates of the two flue gases are gradually reduced, and the reaction is gradually promoted.
In addition, the flow rates of the two flue gases may also be 2m/s, 4m/s, 5m/s, 6m/s, 8m/s, 10m/s, 11m/s, 12m/s, 13m/s, etc.
Preferably, as a further implementable scheme, the desulfurizing agent is prepared into an aqueous solution with a mass percentage concentration of 30-80%, preferably prepared into an aqueous solution of the desulfurizing agent with a mass percentage concentration of 75%, and the mass concentration of the sodium hydroxide solution cannot be too low, otherwise the subsequent treatment is not thorough, and certainly the concentration of the sodium hydroxide solution cannot be too high, so as to avoid influencing the uniformity of gas-liquid two-mixing reaction after the sodium hydroxide solution is contacted with the flue gas.
The chemical reaction principle of the two kinds of smoke is as follows:
in VOCs gas, formaldehyde generates hydroxymethanesulfonic acid (for producing medicines of neoarsine and sodium isoniazid sulfonate and electroplating additive intermediate) by absorbing sulfur dioxide, and the chemical equation is as follows:
SO2+H2O+HCHO＝CH4SO4
if the subsequent treatment is not complete, a desulfurizer is added for continuous treatment, and the disproportionation reaction of formaldehyde and the desulfurizer (sodium hydroxide) is carried out to generate methanol CH3OH and sodium formate HCOONa, the sodium benzoate produced is also a valuable product, and can be used as preservative of pharmaceutical preparationAn agent having the chemical formula:
2HCHO+NaOH＝HCOONa+CH3OH
in the VOCs gas, phenol is removed by the following method, sodium phenolate reacts with sulfur dioxide to generate carbolic acid (acid) and sodium sulfite (cellulose sulfite, organic chemicals, bleaching fabrics and the like, and is also used as a reducing agent, a preservative and a dechlorinating agent):
SO2+H2O+2C6H5ONa＝2C6H5OH+Na2SO3
if the treatment is not complete, a desulfurizing agent is added for continuous treatment, and the reaction equation of phenol and the desulfurizing agent (sodium hydroxide) is as follows:
C6H5OH+NaOH＝C6H5ONa+H2O
in the VOCs gas, methane is removed by the following method, and the reaction equation of the total methane hydrocarbon and sulfur dioxide is as follows: CH (CH)4+SO2＝CO2+2H2+S
The methane and nitric oxide undergo oxidation-reduction reaction, and the specific reaction equation is as follows:
4NO+CH4＝2N2+CO2+2H2O
the specific equation for the reaction of methane with nitrogen dioxide is as follows:
CH4+4NO2═4NO+CO2+2H2O
in a word, by adopting the reaction principle, the two kinds of flue gas react after being mixed, so that most of the flue gas can be subjected to harmless treatment, the flue gas can react with the added desulfurizer to continue the harmless treatment under the condition of incomplete treatment, and the whole treatment method finally realizes the complete treatment of all the flue gas.
The utility model discloses except providing a method of handling VOCs gas, still provide the gaseous treatment facility of a complete set of VOCs, include:
the pre-reaction tank is used for the intermixing reaction of the flue gas of the cupola furnace and the flue gas of the incinerator;
a gas catcher for further catching of flue gas;
the desulfurization reaction tank is used for the intermixing reaction of a desulfurizing agent and flue gas; a desulfurizer spraying device is arranged at the top of the desulfurization reaction tank;
the pre-reaction tank, the gas catcher and the desulfurization reaction tank are sequentially connected.
The utility model discloses a VOCs gas treatment facility simple structure only needs simple three equipment just can realize the abundant processing of flue gas, and the preferred shower head that is preferred to desulfurizer spray set in the desulfurization retort sprays the desulfurizer aqueous solution that gets off through the shower head and the mixed reaction of flue gas, absorbs the processing to the flue gas.
Preferably, as a further implementable scheme, the top of the pre-reaction tank is connected with a cupola flue gas pipeline and an incinerator flue gas pipeline which are arranged side by side, and the diameter of the incinerator flue gas pipeline is 2 times that of the cupola flue gas pipeline.
Preferably, as a further implementable scheme, a plurality of layers of grating plates are distributed in the gas catcher, and the grating plates are arranged to reduce the flow velocity of the flue gas, increase the contact area between the flue gases and improve the treatment effect.
Preferably, as a further implementable scheme, the top of the desulfurization reaction tank is connected with an induced draft fan for promoting the flow of the flue gas in the desulfurization reaction tank.
Preferably, as a further implementable scheme, a material outlet is formed in the bottom of the desulfurization reaction tank, the material outlet is connected with a filter press, and a conveying pump is preferably arranged between the material outlet and the filter press.
The desulfurization, denitrification and dedusting flue gas of the cupola furnace and the VOCs flue gas enter a pre-reaction tank for mixed reaction simultaneously to ensure that the flue gas SO of the cupola furnace is subjected to mixed reaction2、NOXWith incinerator flue gas HCHO, C6H5-OH、CH4And reacting to respectively generate pollution-free substances. The flue gas which is not completely reacted enters a gas catcher and a desulfurization reaction tank in sequence to be continuously reacted to generate pollution-free substancesThe pollution-free substances enter a filter press through a material outlet to be subjected to water-sewage separation, and are preferably pumped into the filter press through a feed pump to be subjected to water-sewage separation SO as to remove TSP and SO2、NOX、HCHO、C6H5-OH、CH4The purpose of smoke pollutants.
In summary, the following description is made for the specific design of the process for removing VOCs from formaldehyde, phenol and methane total hydrocarbons and the equipment for removing VOCs:
a cupola flue gas pipeline and an incinerator flue gas pipeline are arranged at an inlet at the top of the pre-reaction tank side by side, the cupola flue gas and the incineration curing furnace flue gas are fully mixed in the pre-reaction tank to generate chemical reaction, sulfur dioxide respectively reacts with formaldehyde, phenol and methane total hydrocarbon, and simultaneously hydroxymethanesulfonic acid, carbolic acid (acid) and sodium sulfite as well as carbon dioxide, nitrogen, nitric oxide, nitrogen dioxide and methane total hydrocarbon are respectively generated to generate nitrogen and water.
Then, the formaldehyde and phenol flue gas which are not completely removed enter a desulfurization reaction tank to react with sodium hydroxide serving as a desulfurizing agent to generate methanol CH3OH, sodium formate HCOONa and sodium phenolate C6H5ONa, which enters a filter press along with sewage to separate the sewage and achieve the purpose of removing!
Preferably, the sectional area of the pre-reaction tank is 2 (the sectional area of the flue gas pipeline of the cupola furnace + the sectional area of the flue gas pipeline of the incinerator), so that the flow speed of the mixed flue gas is reduced by one time, and the flue gas is fully mixed and fully reacted. Can fall into the bottom of the pre-reaction tank along with the centrifugal force of the induced draft fan and the gravity of the flue gas vertically, the pre-reaction tank is communicated with the upper part of the gas catcher, the flue gas is fully mixed when entering the gas catcher through the pre-reaction tank, and the flue gas phase and the VOC are realizedSGas phase chemical reaction. At first, the flow velocity of two streams of flue gas is controlled at 15m/s, after the flue gas enters a pre-reaction tank, the sectional area of the pre-reaction tank is twice of the sum of the sectional areas of two pipelines, the flow velocity of the flue gas is reduced to 7.5m/s, the flue gas is fully mixed, and then the flow velocity is reduced to 3m/s after the flue gas enters a gas catcher, so that the flue gas can be more fully reacted, the flue gas which is not reacted enters a desulfurization reaction tank to react with sodium hydroxide, and formaldehyde and benzene are secondarily removedPhenol can basically remove 100% of harmful substances in the flue gas, and the finally treated flue gas is discharged from the bottom of the desulfurization reaction tank.
Compared with the prior art, the beneficial effects of the utility model reside in that:
(1) the utility model discloses an utilize flue gas to handle VOCSThe method for preparing the flue gas comprises the step of mixing and reacting the flue gas of the cupola furnace with the flue gas of the incinerator to ensure that SO in the flue gas of the cupola furnace2、NOXHCHO and C in the smoke of the incinerator and the same components6H5-OH、CH4The components are reacted, and after the reaction is completed, pollution-free products are respectively generated, so that the method is simple and the cost is low;
(2) the treatment method of the utility model achieves scientific treatment of VOCs gas and toxic gas containing nitrogen and sulfur, has strong operability and can realize industrialized operation;
(3) the utility model discloses a VOCSThe gas treatment equipment has a simple structure, less three wastes, realizes full reaction treatment of the flue gas, occupies small area, and is green and environment-friendly;
(4) the utility model discloses a VOCSThe gas treatment equipment can realize 100% treatment of the cupola flue gas and the incinerator flue gas, and extra treatment equipment is not needed to be added subsequently, so that the operation steps are simplified, and the operation cost is reduced.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of a processing apparatus for processing VOCs gas by using flue gas provided by the embodiment of the present invention.
Description of the drawings:
10-a pre-reaction tank; 101-cupola flue gas duct;
102-incinerator flue gas duct; 20-a gas trap;
201-a grid plate; 30-a desulfurization reaction tank;
301-desulfurizer spray device; 302-material outlet;
40-a filter press; 50-a delivery pump;
and 60-an induced draft fan.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings and detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to clarify the technical solution of the present invention, the following description is made in the form of specific embodiments.
Examples
Referring to fig. 1, a cupola flue gas pipeline 101 and an incinerator flue gas pipeline 102 are arranged at the top inlet of a pre-reaction tank 10 side by side, the diameter of the incinerator flue gas pipeline 102 is 2 times of the diameter of the cupola flue gas pipeline 101, the two pipelines simultaneously extend into the pre-reaction tank 10, so that cupola flue gas and incineration curing furnace flue gas enter the pre-reaction tank 10 to be fully mixed according to the volume ratio of 1:2, chemical reaction is carried out, sulfur dioxide respectively reacts with formaldehyde, phenol and methane total hydrocarbon, and simultaneously hydroxymethanesulfonic acid, carbolic acid (acid), sodium sulfite, carbon dioxide, nitrogen, nitric oxide, nitrogen dioxide and methane total hydrocarbon are respectively generated to generate nitrogen and water, and the sectional area of the pre-reaction tank 10 is 2 times of the sum of the sectional areas of the cupola flue gas pipeline 101 and the incinerator flue gas pipeline 102.
At first, the flow rate of the flue gas of the cupola furnace flowing through the flue gas pipeline 101 of the cupola furnace is controlled to be 15m/s, the flow rate of the flue gas of the incinerator flowing through the flue gas pipeline 102 of the incinerator is also controlled to be 15m/s, after the two flue gases enter the pre-reaction tank 10, the flow rate of the flue gases is reduced to 7.5m/s, the two flue gases are fully mixed, generally, the sectional area of the pre-reaction tank 10 is 2 (the sectional area of the flue gas pipeline 101 of the cupola furnace and the sectional area of the flue gas pipeline 102 of the incinerator), so that the flow rate of the mixed flue gases is reduced by one time, and full mixing and full.
The pre-reaction tank 10 is preferably provided with an induced draft fan 60, so that the flue gas can vertically fall into the bottom of the pre-reaction tank 10 along with the centrifugal force of the induced draft fan 60 and the gravity of the flue gas, the pre-reaction tank 10 is communicated with the upper part of the gas catcher 20, the flue gas is fully mixed when entering the gas catcher 20 through the pre-reaction tank 10, and the gas phase of the flue gas is realizedAnd VOCSGas phase chemical reaction. In order to reduce the flow velocity of the flue gas, a plurality of layers of grid plates 201 are vertically arranged in the gas catcher 20. The flow velocity of the flue gas in the gas trap 20 is 3 m/s.
Then, the formaldehyde and phenol fume which are not completely removed enter a desulfurization reaction tank 30 to react with sodium hydroxide serving as a desulfurizing agent to generate methanol CH3OH, sodium formate HCOONa and sodium phenolate C6H5ONa, the substances enter the filter press machine 40 together with the sewage from the material outlet 302 at the bottom of the desulfurization reaction tank 30 for water-sewage separation, so as to achieve the purpose of removal. The top of the desulfurization reaction tank 30 is provided with a desulfurizer spray device 301, the desulfurizer spray device 301 is in a spray header structure, and the desulfurizer sodium hydroxide is prepared into an aqueous solution with the mass percentage concentration of 75 wt%, and is sprayed by the spray header and reversely contacted with the flue gas for absorption.
An induced draft fan 60 for promoting the flow of the flue gas in the desulfurization reaction tank 30 is disposed at the top of the desulfurization reaction tank 30, and a transfer pump 50 is further disposed between the material outlet 302 and the filter press 40.
In the above embodiment, the volume ratio of the cupola flue gas to the incinerator flue gas may also be 1:1.8, 1:1.9, 1:2.5, and so on.
In the above embodiment, the desulfurizing agent may be potassium hydroxide, or a mixture of sodium hydroxide and potassium hydroxide, besides sodium hydroxide, and the mass percentage concentration of the desulfurizing agent aqueous solution may also be 30%, 80%, and so on.
In the above described embodiments, the flow velocity of the flue gas within the gas trap 20 may also be 1 m/s.
Application example
Ultra-low design parameters: flue gas flow of cupola furnace is 2 ten thousand meters3H; the concentration of particulate matters in the flue gas is 2000mg/m3The concentration of nitrogen oxide in the flue gas is 500mg/m3The concentration of sulfur dioxide in the flue gas is 1110mg/m3。
Flue gas flow of cotton collecting and solidifying incinerator is 4 ten thousand meters3H, 3.03mg/m of formaldehyde in flue gas3(ii) a Flue gas phenol 2.12mg/m3(ii) a Flue gas methane total hydrocarbon 5.15mg/m3。
The exhaust gas parameters were as follows:
rated energy consumption of the cupola:
120 ten thousand meters3A natural gas; 12000T/a of coke; electricity 905 ten thousand kwh/a; fresh water 18327T/a
Total flue gas amount of cupola furnace 20000+ total flue gas amount of incinerator 4000Nm3H (standard condition)
Quantity: cupola, cotton collecting production line and curing production line
The operation mode is as follows: all the year round.
VOC removalSThe sulfur dioxide in the flue gas is needed, and the method is a rich chemical reaction.
The reaction was rich in 22.22kg of sulfur dioxide produced per hour and 1.02kg of sulfur dioxide was used.
10kg of nitrogen oxides were formed per hour, and 0.74kg of nitrogen oxides was used as a rich reaction, and the ratios of the specific treatment materials were as shown in tables 1 to 4 below.
TABLE 1 pollutant flow
| Name of contaminant | Flue gas flow m3/h | Concentration mg/m3 | kg/h | Using the ratio of sulfur dioxide | SO2(kg) |
| Hourly production of sulfur dioxide | 20000 | 1111 | 22.22 | ||
| Amount of Formaldehyde produced per hour | 40000 | 3.03 | 0.1212 | 2.00 | 0.242 |
| Hourly phenol formation | 40000 | 2.12 | 0.0848 | 0.37 | 0.031 |
| Hourly methane formation | 40000 | 5.15 | 0.2060 | 3.60 | 0.742 |
| Total mass kg/h of VOCS | 0.4120 | 1.015 | |||
| Name of contaminant | Flue gas flow m3/h | Concentration mg/m3 | kg/h | Using nitrogen oxides kg/h | |
| Hourly production of nitrogen oxides | 20000 | 500 | 10 | ||
| Hourly methane formation | 40000 | 5.15 | 0.2 | 3.60 | 0.7416 |
TABLE 2 desulfurizing agent requirement
| Name of contaminant | Flue gas flow m3/h | Concentration mg/m3 | kg/h | Using sodium hydroxide multiple | NaOH(kg) |
| Amount of Formaldehyde produced per hour | 40000 | 3.03 | 0.1212 | 1.09 | 0.1321 |
| Hourly phenol formation | 40000 | 2.12 | 0.0848 | 0.42 | 0.0356 |
| Total (kg) | 0.1677 |
TABLE 3 use amount of desulfurizing agent for removing VOCs
| Contaminants | Weight kg/h of pollutants | Using sulfur dioxide kg/h | Sodium hydroxide is used in kg/h |
| Removal of formaldehyde | 0.12 | 0.07 | 0.08 |
| Removal of phenol | 0.08 | 0.03 | 0.08 |
| Removal of methane total hydrocarbons | 0.2 | 0.05 | |
| Total up to | 0.4 | 0.15 | 0.16 |
| Removal of methane total hydrocarbons | Using nitrogen oxides kg/h | ||
| Total up to | 0.2 | 1 |
TABLE 4 use amount of desulfurizing agent for removing sulfur dioxide
| Name of contaminant | Flue gas flow m3/h | Concentration mg/m3 | SO2,kg/h | Using sodium hydroxide in kg by mass |
| Hourly production of sulfur dioxide | 20000 | 1111 | 22.22 | 33.3 |
| Using the total amount of sodium hydroxide | 33.5 |
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (8)
1. An apparatus for treating VOCs gas with flue gas, comprising:
the pre-reaction tank is used for the intermixing reaction of the flue gas of the cupola furnace and the flue gas of the incinerator;
a gas catcher for further catching of flue gas;
the desulfurization reaction tank is used for the intermixing reaction of a desulfurizing agent and flue gas; a desulfurizer spraying device is arranged at the top of the desulfurization reaction tank;
the pre-reaction tank, the gas catcher and the desulfurization reaction tank are sequentially connected.
2. The apparatus for treating VOCs gas by using flue gas according to claim 1, wherein the top of the pre-reaction tank is connected with a cupola flue gas pipeline and an incinerator flue gas pipeline which are arranged side by side, and the diameter of the incinerator flue gas pipeline is 2 times of that of the cupola flue gas pipeline.
3. The apparatus according to claim 1, wherein a plurality of grid plates are disposed in the gas trap.
4. The apparatus for treating VOCs gas by using flue gas according to claim 1, wherein an induced draft fan for promoting the flow of flue gas in the desulfurization reaction tank is connected to the top of the desulfurization reaction tank.
5. The apparatus for treating VOCs gas by using flue gas according to claim 1, wherein a material outlet is arranged at the bottom of the desulfurization reaction tank, and a filter press is connected to the material outlet.
6. The apparatus according to claim 5, wherein a transfer pump is disposed between the material outlet and the filter press.
7. The apparatus for treating VOCs gas by using flue gas according to claim 2, wherein the sectional area of the pre-reaction tank is 2 times of the sum of the sectional areas of the cupola flue gas duct and the incinerator flue gas duct.
8. The apparatus according to claim 1, wherein the desulfurizer spray device is a spray head structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020589234.5U CN212167011U (en) | 2020-04-20 | 2020-04-20 | Equipment for treating VOCs gas by using flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020589234.5U CN212167011U (en) | 2020-04-20 | 2020-04-20 | Equipment for treating VOCs gas by using flue gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212167011U true CN212167011U (en) | 2020-12-18 |
Family
ID=73766638
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020589234.5U Active CN212167011U (en) | 2020-04-20 | 2020-04-20 | Equipment for treating VOCs gas by using flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212167011U (en) |
-
2020
- 2020-04-20 CN CN202020589234.5U patent/CN212167011U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11014044B2 (en) | Waste gas purification system and method | |
| Guo et al. | Applications of high-gravity technologies in gas purifications: A review | |
| CN103721550B (en) | Flue gas and desulfurizing and denitrifying takes off VOCs absorbent and preparation thereof and application | |
| CN203750409U (en) | Flue gas purifying treatment device in waste incineration process | |
| CN102489149A (en) | Flue-gas purification and reclamation system and method thereof | |
| CN103055675A (en) | Industrial smoke comprehensive treatment system and method based on advanced oxidation | |
| CN108295565A (en) | The method and system of flue gas desulfurization and denitrification | |
| JP2014024052A (en) | Fly ash circulation type exhaust gas treatment method | |
| CN106390741A (en) | H2O2-catalytic-oxidation-based system and method for removing NO, SO2 and Hg0 in flue gas | |
| CN205055820U (en) | Purification treatment system of msw incineration tail gas | |
| CN211358310U (en) | Waste water zero release flue gas ultra-clean processing system of waste incinerator | |
| WO2018192564A1 (en) | Flue gas purification system for domestic waste pyrolysis incinerator | |
| CN107485999A (en) | The processing method of flue gas of refuse burning | |
| CN105381699B (en) | A kind of hydrogen peroxide oxidation joint amino wet desulphurization method of denitration and its device | |
| CN105126564B (en) | The method and apparatus of flue gas and desulfurizing and denitrifying | |
| CN212167011U (en) | Equipment for treating VOCs gas by using flue gas | |
| CN211612184U (en) | Treatment device for waste gas in tar treatment process | |
| CN106139840A (en) | Purifier and method containing low concentration VOC waste gas | |
| JP7316146B2 (en) | Dilute sulfuric acid production apparatus and dilute sulfuric acid production method | |
| CN107551779A (en) | The processing unit of flue gas of refuse burning | |
| CN111036039A (en) | Treatment device and treatment method for waste gas in tar treatment process | |
| CN111359407A (en) | Method and equipment for treating VOCs gas by using flue gas | |
| CN105709595A (en) | System and method for synchronously performing low-temperature denitration and desulfuration on coke oven smoke | |
| CN107185398A (en) | A kind of system and its method of work for administering boiler smoke | |
| CN205216553U (en) | Hydrogen peroxide solution deNOx systems |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |