CN210814655U - Tail gas treatment system of fluorescent brightener sulfur oxidation coupling reaction section - Google Patents
Tail gas treatment system of fluorescent brightener sulfur oxidation coupling reaction section Download PDFInfo
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- CN210814655U CN210814655U CN201921038332.3U CN201921038332U CN210814655U CN 210814655 U CN210814655 U CN 210814655U CN 201921038332 U CN201921038332 U CN 201921038332U CN 210814655 U CN210814655 U CN 210814655U
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- tail gas
- sodium hydroxide
- coupling reaction
- hydrogen sulfide
- oxidation coupling
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Abstract
The utility model discloses a tail gas processing system of fluorescent brightener sulphur oxidation coupling reaction workshop section, the tail gas processing system of fluorescent brightener sulphur oxidation coupling reaction workshop section, including sodium hydroxide tail gas absorption tank I of one-level absorption hydrogen sulfide, sodium hydroxide tail gas absorption tank I even has the sodium hydroxide tail gas absorption tank II of further absorption hydrogen sulfide, sodium hydroxide tail gas absorption tank II even has the spray column of further absorption hydrogen sulfide, the spray column even has the active carbon adsorption equipment who adsorbs hydrogen sulfide. The utility model discloses a set up sodium hydroxide tail gas absorption jar I and sodium hydroxide tail gas absorption jar II two-stage tail gas absorption and assist the spray column absorption, still reduce the load that later stage hydrogen sulfide further got rid of when fully absorbing the hydrogen sulfide in the tail gas to obtain sodium sulfide solution by-product, assist at last with the hydrogen sulfide further absorption of active carbon adsorption device in to the tail gas, make the hydrogen sulfide content in the tail gas reach emission standard, reduce and pollute with the hydrogen sulfide.
Description
Technical Field
The utility model relates to a fluorescent brightener production facility technical field, concretely relates to fluorescent brightener sulphur oxidation coupling reaction workshop section's tail gas treatment system.
Background
Fluorescent brightener production process mainly includes condensation reaction, sulfur oxidation coupling reaction, three big reaction workshop sections of refining process, the utility model provides a reaction system is used for sulfur oxidation coupling reaction wherein, and its effect is turned into the fluorescent brightener crude product with 2-p-tolyl benzoxazole midbody and the sulphur that the condensation reaction workshop section obtained, the utility model relates to a workshop section is enlargied by laboratory lab scale and is formed, and main reaction equipment is miniature reation kettle, and the aftertreatment relates to the suction filtration device, and waste gas, the waste water that produces in the experimentation is less, and is less to environmental impact, general direct emission. However, after the production is enlarged, especially the production capacity of 1000 tons/year is large, hydrogen sulfide gas generated in the reaction process and filtrate generated by suction filtration cannot be directly discharged, the existing test device is difficult to effectively treat and apply waste gas and waste liquid generated in the reaction process, the environmental pollution is large in the production process, the unit consumption of raw materials is high, and the overall economic benefit is influenced, so that the reaction system suitable for the sulfur oxidation coupling reaction section of the fluorescent whitening agent is provided, and the reaction system has great significance for the industrial production of the fluorescent whitening agent.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: the tail gas treatment system for the sulfur oxidation coupling reaction section of the fluorescent whitening agent is used for industrial production of the fluorescent whitening agent, and solves the problem that the tail gas treatment system for the sulfur oxidation coupling reaction section of the existing fluorescent whitening agent cannot effectively treat and apply waste gas and liquid.
In order to achieve the above object, the utility model adopts the following technical scheme:
the tail gas treatment system of the fluorescent brightener sulfur oxidation coupling reaction section comprises a sodium hydroxide tail gas absorption tank I which absorbs hydrogen sulfide at one level, wherein the sodium hydroxide tail gas absorption tank I is connected with a sodium hydroxide tail gas absorption tank II which further absorbs hydrogen sulfide, the sodium hydroxide tail gas absorption tank II is connected with a spray tower which further absorbs hydrogen sulfide, and the spray tower is connected with an active carbon adsorption device which adsorbs hydrogen sulfide.
Preferably, a pipeline for conveying liquid from the sodium hydroxide tail gas absorption tank II to the sodium hydroxide tail gas absorption tank I is connected between the sodium hydroxide tail gas absorption tank I and the sodium hydroxide tail gas absorption tank II, the sodium hydroxide tail gas absorption tank I is connected with a liquid output pipeline, and the sodium hydroxide tail gas absorption tank II is connected with a liquid input pipeline.
Preferably, a liquid output pipeline of the sodium hydroxide tail gas absorption tank I is connected with a sodium sulfide concentration increasing system, the sodium sulfide concentration increasing system comprises a washing kettle used for reaction of sodium sulfide and sulfur, the washing kettle is connected with a condenser II used for condensing waste gas generated in the reaction process and a solid-liquid separation device used for solid-liquid separation, and the condenser II is connected with a solvent recovery container used for storing a solvent obtained by condensation.
Preferably, solid-liquid separation equipment includes the suction filtration bucket, the suction filtration bucket even has the suction filtration cauldron that is used for bleeding and handles filtrating, the suction filtration cauldron even has the activated carbon filter with filtrating decoloration and circulates the circulating pump between suction filtration cauldron, filter with filtrating. The arranged active carbon filter can effectively remove the variegated color in the filtrate (sodium sulfide solution) and improve the product phase of the by-product of the sodium sulfide solution.
Preferably, the washing kettle and the suction filtration kettle are both set as enamel reaction kettles.
Preferably, the material of the suction filter barrel is carbon steel.
Preferably, the suction filtration kettle is connected with an alkali liquor storage device.
Preferably, the lye storage device is provided as a carbon steel storage tank.
Preferably, the solvent recovery vessel is a sealed bucket or a sealed tank.
Preferably, the activated carbon adsorption device is connected with a 25m high exhaust funnel for discharging exhaust gas.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model has the advantages that the tail gas absorption of the two stages of the sodium hydroxide tail gas absorption tank I and the sodium hydroxide tail gas absorption tank II is arranged and is assisted by the absorption of the spray tower, so that the hydrogen sulfide in the tail gas is fully absorbed, and the load of further removing the hydrogen sulfide in the later stage is reduced; sodium sulfide solution byproducts meeting the selling conditions can be obtained, and the economic benefit is increased; finally, an activated carbon adsorption device is used for further absorbing the hydrogen sulfide in the tail gas, so that the content of the hydrogen sulfide in the tail gas reaches the emission standard, and the pollution caused by the hydrogen sulfide is reduced;
2. the utility model discloses a set up sodium sulfide concentration lift system, can promote 350g/l by original concentration with sodium sulfide concentration at 300g/l, and the totality does not influence the recovery of low reaches production sodium bicarbonate (sodium thiosulfate) sodium sulfide producer, still can apply originally dumped sulphur, wash sulphur through adopting to retrieve sodium sulfide solution, improve the concentration of retrieving sodium sulfide solution, the fluorescent brightener crude product that will not be dissolved in sodium sulfide solution washes out, thereby reach the purpose that improves fluorescent brightener crude product purity.
3. The utility model discloses a set up sodium sulfide concentration lift system, calculate according to every batch washing 300Kg waste gas sulphur, apply mechanically and contain fluorescent whitening agent crude product volume 10% in the sulphur, about containing 30 kilograms fluorescent whitening agent crude product in every batch 300KG sulphur that applies mechanically, can obtain embodying in next batch yield after applying mechanically, 20 batches are washd in the plan of a year, obtain 600 kilograms fluorescent whitening agent crude product, compare in abandonment the sulphur, fluorescent whitening agent crude product total output has increased 600 kilograms.
Drawings
FIG. 1 is a schematic diagram showing the connection relationship of various devices in a production system of a sulfur oxidation coupling reaction section of a fluorescent whitening agent according to an embodiment of the present invention;
FIG. 2 is a schematic diagram showing the connection relationship between the devices of the sodium sulfide concentration raising system;
FIG. 3 is a schematic flow chart of the production process of the sulfur oxidation coupling reaction section of the fluorescent whitening agent provided by the embodiment of the present invention.
Wherein, the names corresponding to the reference numbers are:
1. sulfur oxidizing the coupling kettle; 2. a sodium hydroxide tail gas absorption tank I; 3. a sodium hydroxide tail gas absorption tank II; 4. a spray tower; 5. an activated carbon adsorption unit; 6. a suction filtration device; 7. a sulfur still; 8. a condenser I; 9. a finished sulfur product boiler; 10. a sulphur slicing device; 11. washing the kettle; 12. a suction filtration barrel; 13. a suction filtration kettle; 14. a circulation pump; 15. an activated carbon filter; 16. a condenser II; 17. a solvent recovery vessel.
Detailed Description
The present invention will be further described with reference to the following description and examples, which include but are not limited to the following examples.
As shown in figure 1, the production system for the sulfur oxidation coupling reaction section of the fluorescent whitening agent has the advantages of simple structure, scientific and reasonable design, convenience in use, high waste gas purification efficiency and ideal waste gas purification effect, the discharged waste gas can reach the waste gas emission standard, and the solvent recycling structure is arranged for multiple times, so that the use amount of the solvent can be greatly reduced, the unit consumption of the solvent is reduced, and the overall economic benefit is improved.
The production system of the fluorescent brightener sulfur oxidation coupling reaction section comprises a sulfur oxidation coupling kettle 1 for sulfur oxidation coupling reaction, wherein the sulfur oxidation coupling kettle 1 is connected with a sodium hydroxide tail gas absorption tank I2 for absorbing hydrogen sulfide and a suction filtration device 6 for suction filtration of a fluorescent brightener crude product, the sodium hydroxide tail gas absorption tank I2 is connected with a sodium hydroxide tail gas absorption tank II3 for further absorbing hydrogen sulfide, the sodium hydroxide tail gas absorption tank II3 is connected with a spray tower 4 for further absorbing hydrogen sulfide, and the spray tower 4 is connected with an active carbon adsorption device 5 for adsorbing hydrogen sulfide; the suction filtration device 6 is connected with a sulfur still 7 for processing filtrate, the sulfur still 7 is connected with a condenser I8 for condensing solvent and a sulfur finished product pot 9, the condenser I8 is connected with a return pipeline for returning the solvent to the sulfur oxidation coupling kettle 1, and the sulfur finished product pot 9 is connected with a sulfur slicing device 10 for slicing sulfur.
The condenser I8 is a water-cooled condenser.
The activated carbon adsorption device 5 is connected with a 25m high exhaust funnel for discharging exhaust gas.
The suction filtration device 6 comprises a closed suction filtration tank below the sulfur oxidation coupling kettle 1, and the sulfur oxidation coupling kettle 1 is connected with the closed suction filtration tank through a pumping pipeline.
The sulfur distillation kettle 7 is connected with the sulfur product pot 9 through a pipeline air compression material pipe, and a material pressing valve is arranged on the pipeline air compression material pipe.
The sulfur distillation kettle 7 is connected with a vacuum pump for pumping out non-condensable gas, and the vacuum pump is connected with an activated carbon adsorption device for waste gas adsorption.
A pipeline for conveying liquid from the sodium hydroxide tail gas absorption tank II3 to the sodium hydroxide tail gas absorption tank I2 is connected between the sodium hydroxide tail gas absorption tank I2 and the sodium hydroxide tail gas absorption tank II3, the sodium hydroxide tail gas absorption tank I2 is connected with a liquid output pipeline, and the sodium hydroxide tail gas absorption tank II3 is connected with a liquid input pipeline. The addition and the transfer of the alkali liquor and the full absorption of the alkali liquor are convenient.
As shown in fig. 2, for the utility model provides a sodium sulfide concentration lift system for handle sodium sulfide solution that sodium hydroxide tail gas absorption jar I and sodium hydroxide tail gas absorption jar II obtained and apply mechanically sulphur many times, the investment is less, can improve fluorescent whitening agent's quality yield, reduces exhaust emissions, increases the sodium sulfide and retrieves, reduces solid useless, brings considerable benefit for the enterprise.
A sodium sulfide concentration lift system for optical brightener production, including the washing kettle 11 that is used for sodium sulfide and sulphur reaction, washing kettle 11 even has the condenser II16 that is used for the waste gas of condensation reaction process production and is used for solid-liquid separation's solid-liquid separation equipment, condenser II16 even has the solvent recovery container 17 of the solvent that the storage condensation obtained, solid-liquid separation equipment is including suction filtration bucket 12, suction filtration bucket 12 even has the suction filtration cauldron 13 that is used for bleeding and handles filtrating, suction filtration cauldron 13 even has the active carbon filter 15 with the filtrating decoloration and circulates the circulating pump 14 between suction filtration cauldron 13, filter 15 with the filtrating.
Wherein, the washing kettle 11 and the suction filtration kettle 13 are both set as enamel reaction kettles; the material of the suction filtration barrel 12 is carbon steel.
In order to prevent the shutdown caused by the sodium sulfide recovery liquid expansion warehouse in the tail gas absorption area due to insufficient operation of downstream sodium sulfide factories, the suction filtration kettle 13 is connected with an alkali liquor storage device which is a carbon steel storage tank.
Condenser II16 is water-cooled condenser, adopts circulating water cooling, sets up 1 cooling tower.
The solvent recovery container 17 is a sealed barrel or a sealed tank, so that the volatilization of the recovered solvent is avoided, and the unorganized emission of the solvent is reduced.
The specific working flow of the sodium sulfide concentration increasing system is as follows:
a. in the washing kettle, 3 batches of the recovered sodium sulfide solution, 2 tons for each batch, were put in, and 6 tons in total were put in, and 300KG of the recovered sulfur was put in.
b. The recovered sodium sulfide solution was originally kept at 60 degrees, and after sulfur was added, the temperature was raised to 80 degrees, and the mixture was stirred for 1 hour.
c. The solution is pumped to a suction filtration kettle through a suction filtration tank by vacuum, and the impure color in the filtrate (sodium sulfide solution) is removed through an active carbon filter, so that the product phase of the sodium sulfide solution by-product is improved.
d. The crude fluorescent whitening agent in the suction filtration tank is used for refining in the next working procedure, and the sodium sulfide solution in the suction filtration kettle and other recovered sodium sulfide solutions are sent to nearby sodium sulfide factories.
The reaction equation is as follows:
NaOH+S→Na2S+Na2S2O3+H2O
NaS+S→Na2S2
as shown in fig. 3, a schematic production flow diagram of the sulfur oxidation coupling reaction section of the fluorescent whitening agent produced by the present invention is shown, and the specific production flow is as follows:
putting the sulfur and the crude product of 2-p-tolyl benzoxazole into a 2000L sulfur oxidation coupling kettle (heat source adopts heat conducting oil) by adopting a small crane according to the ratio of 2:1, and opening H under the protection of nitrogen2S absorption device, slowly heating to 240 deg.C, keeping the temperature, and reacting for 18 hr to obtain H2And (3) preparing the sodium sulfide by absorbing the S gas by 30% liquid caustic soda 2. The residual small amount of unreacted hydrogen sulfide waste gas is absorbed by a spray tower and an active carbon adsorption device in two stages, and the final hydrogen sulfide waste gas G5 reaching the discharge standard and discharging through a 25m high exhaust funnel.
Wherein H2The S gas treatment process specifically comprises the following steps: h2S gas sequentially enters a 3000L sodium hydroxide tail gas absorption tank I2 and a sodium hydroxide tail gas absorption tank II3 through a buffer tank to be absorbed, liquid caustic soda in the sodium hydroxide tail gas absorption tank I2 and the sodium hydroxide tail gas absorption tank II3 is a 30% sodium hydroxide solution, the sulfur absorption concentration of the sodium hydroxide tail gas absorption tank I2 reaches 350g/L, the absorption rate of each stage of alkali liquor is greater than 90% at the absorption end point, the sulfur concentration of the sodium hydroxide tail gas absorption tank II3 is about 30g/L at the moment, the liquid caustic soda in the sodium hydroxide tail gas absorption tank I2 is transferred out, the liquid caustic soda in the sodium hydroxide tail gas absorption tank II3 is transferred into the sodium hydroxide tail gas absorption tank I2, the liquid caustic soda is added into the sodium hydroxide tail gas absorption tank II3 again, and absorption is continued. The spray liquid of the spray tower is 30% sodium hydroxide solution, and the absorbed sodium sulfide-containing wastewater is completely added into the sodium sulfide solution and is not discharged outside. At present, the concentration of sulfur in the sodium sulfide solution exceeds 300g/L and reaches the sale standard, while the concentration of the sodium sulfide obtained by the project is about 300 g/L-325 g/L and can be sold to Ningxia units according to byproducts. The Alxa-levo-flag Min Shunhu chemical industry Limited company has signed a supply agreement with Ningxia Lanfeng fine chemical industry Limited company, the Ningxia Lanfeng fine chemical industry Limited company needs sodium sulfide for production, the absorption of hydrogen sulfide gas is finished, and when sodium sulfide solution is put into the Ningxia Lanfeng fine chemical industry Limited company, a very small amount of hydrogen sulfide g3 is discharged disorderly.
After the sulfur oxidation coupling reaction is finished, cooling to 160 ℃ by using cold heat conduction oil, adding dimethylbenzene into a sulfur oxidation coupling kettle to dissolve the dimethylbenzene, and continuously cooling to 140 ℃.
And after cooling, pumping the material and the solution into a closed pumping filtration tank below the bottom of the sulfur oxidation coupling kettle through a closed pipeline, and performing pumping filtration at 140 ℃ to obtain a filter cake, namely a crude product of the fluorescent brightener. And (4) covering the upper part of the suction filtration tank, sealing the discharge during discharging, and opening the cover during discharging.
The method comprises the steps of pumping filtrate into a 2000L sulfur distillation kettle (heat source adopts heat conduction oil) through a closed pipeline, closing a material pumping valve, opening a vacuum pump, distilling under negative pressure, slowly heating to 200 ℃, evaporating xylene, condensing and recycling, wherein distillation residual liquid is liquid sulfur, compressing the liquid sulfur into a sulfur finished product pot through nitrogen air pressure, cooling and slicing, recycling sulfur after slicing, sending the recycled liquid sulfur into a sodium sulfide concentration lifting system for 4-5 times, pumping out non-condensable gas g4 through the vacuum pump, and sending waste gas pumped out by the vacuum pump to an active carbon adsorption device through a pipeline.
The condensers involved in the project are all cooled by circulating water and are provided with 1 cooling tower.
The above embodiment is only one of the preferred embodiments of the present invention, and should not be used to limit the protection scope of the present invention, but all the insubstantial changes or modifications made in the spirit and the idea of the main design of the present invention, the technical problems solved by the embodiment are still consistent with the present invention, and all should be included in the protection scope of the present invention.
Claims (10)
1. The tail gas treatment system of the sulfur oxidation coupling reaction section of the fluorescent whitening agent is characterized in that: including sodium hydroxide tail gas absorption tank I (2) of one-level absorption hydrogen sulfide, sodium hydroxide tail gas absorption tank I (2) even have sodium hydroxide tail gas absorption tank II (3) of further absorption hydrogen sulfide, sodium hydroxide tail gas absorption tank II (3) even have spray column (4) of further absorption hydrogen sulfide, spray column (4) even have active carbon adsorption device (5) of absorption hydrogen sulfide.
2. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 1, characterized in that: the device is characterized in that a pipeline which is used for conveying liquid from the sodium hydroxide tail gas absorption tank II (3) to the sodium hydroxide tail gas absorption tank I (2) is connected between the sodium hydroxide tail gas absorption tank I (2) and the sodium hydroxide tail gas absorption tank II (3), the sodium hydroxide tail gas absorption tank I (2) is connected with a liquid output pipeline, and the sodium hydroxide tail gas absorption tank II (3) is connected with a liquid input pipeline.
3. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 2, characterized in that: the liquid output pipeline of sodium hydroxide tail gas absorption tank I (2) even has sodium sulfide concentration lift system, sodium sulfide concentration lift system is including washing cauldron (11) that are used for sodium sulfide and sulphur reaction, washing cauldron (11) even have condenser II (16) that are used for condensing the waste gas that the reaction process produced and the solid-liquid separation equipment who is used for solid-liquid separation, condenser II (16) even have solvent recovery container (17) of the solvent that the storage condensation obtained.
4. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 3, characterized in that: solid-liquid separation equipment is including suction filtration bucket (12), suction filtration bucket (12) even have suction filtration cauldron (13) that are used for bleeding and handle filtrating, suction filtration cauldron (13) even have activated carbon filter (15) with filtrating decoloration and circulate circulating pump (14) between suction filtration cauldron (13), filter (15) with filtrating.
5. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 4, characterized in that: and the washing kettle (11) and the suction filtration kettle (13) are both set as enamel reaction kettles.
6. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 4, characterized in that: the material of the suction filtration barrel (12) is carbon steel.
7. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 4, characterized in that: the suction filtration kettle (13) is connected with an alkali liquor storage device.
8. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 7, characterized in that: the alkali liquor storage device is a carbon steel storage tank.
9. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 3, characterized in that: the solvent recovery container (17) is a sealed barrel or a sealed tank.
10. The tail gas treatment system of a fluorescent brightener sulfur oxidation coupling reaction section as claimed in claim 1, characterized in that: the active carbon adsorption device (5) is connected with a 25m high exhaust funnel for exhausting waste gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921038332.3U CN210814655U (en) | 2019-07-04 | 2019-07-04 | Tail gas treatment system of fluorescent brightener sulfur oxidation coupling reaction section |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921038332.3U CN210814655U (en) | 2019-07-04 | 2019-07-04 | Tail gas treatment system of fluorescent brightener sulfur oxidation coupling reaction section |
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| CN210814655U true CN210814655U (en) | 2020-06-23 |
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| CN201921038332.3U Expired - Fee Related CN210814655U (en) | 2019-07-04 | 2019-07-04 | Tail gas treatment system of fluorescent brightener sulfur oxidation coupling reaction section |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111790172A (en) * | 2020-07-29 | 2020-10-20 | 濮阳市盛源能源科技股份有限公司 | Solvent distillation recovery system and use method |
-
2019
- 2019-07-04 CN CN201921038332.3U patent/CN210814655U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111790172A (en) * | 2020-07-29 | 2020-10-20 | 濮阳市盛源能源科技股份有限公司 | Solvent distillation recovery system and use method |
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Granted publication date: 20200623 Termination date: 20210704 |