CN218222388U - Utilize tail gas processing apparatus of naphthalene method production phthalic anhydride - Google Patents
Utilize tail gas processing apparatus of naphthalene method production phthalic anhydride Download PDFInfo
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- CN218222388U CN218222388U CN202222649659.2U CN202222649659U CN218222388U CN 218222388 U CN218222388 U CN 218222388U CN 202222649659 U CN202222649659 U CN 202222649659U CN 218222388 U CN218222388 U CN 218222388U
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Abstract
The utility model belongs to the technical field of chemical industry equipment, a utilize tail gas processing apparatus of naphthalene method production phthalic anhydride is disclosed, include the light component tower that communicates in proper order with phthalic anhydride preliminary treatment jar, pure phthalic anhydride tower, evaporimeter and residue scrubbing tower, be equipped with light component cooler, pure phthalic anhydride cooler and evaporative condenser in the top of the tower of this three tower respectively, the discharge gate of light component cooler, pure phthalic anhydride cooler and evaporative condenser links respectively with the feed inlet of first air jet pump, second air jet pump and third air jet pump, the discharge gate of this three jet pump communicates the feed inlet of second switching condenser respectively, second switching condenser is equipped with liquid material export and gas material export, its gas material export communicates the incinerator; the discharge ports of the pure phthalic anhydride cooler and the evaporative condenser are also communicated with each other and connected to the feed port of the vacuum condenser, and the discharge port of the vacuum condenser is connected to the phthalic anhydride pretreatment tank. The utility model discloses phthalic anhydride content is low in the tail gas after the processing, has practiced thrift the steam volume, energy saving and consumption reduction.
Description
Technical Field
The utility model belongs to the technical field of chemical industry equipment, concretely relates to utilize tail gas processing apparatus of naphthalene method production phthalic anhydride.
Background
The technological process of preparing phthalic anhydride with naphthalene includes mixing industrial naphthalene and air in certain proportion, oxidizing reaction in a reactor under the action of catalyst to obtain required product phthalic anhydride and side products naphthoquinone and maleic anhydride, gas cooling to exchange heat, condensating in a switching condenser to obtain solid crude phthalic anhydride, and rectifying the crude phthalic anhydride to obtain qualified phthalic anhydride product. In the prior art, a steam jet pump is used for taking steam as a driving air source, phthalic anhydride tail gas generated in the crude phthalic anhydride rectification process is mixed with water vapor and is sent into an incinerator, so that the load of the incinerator is increased, and dust in smoke after incineration pollutes the environment; after the tail gas is extracted by the steam jet pump, the gas is directly discharged into an incineration system, so that phthalic anhydride in the tail gas cannot be recycled for the second time, and resource waste is caused; the steam jet pump can not be normally used due to large heat energy emission amount caused by unstable start-up load and frequent rainstorm in summer, the steam amount is obviously insufficient, and the stable production of the phthalic anhydride is seriously influenced; in the production of 4 ten thousand tons of phthalic anhydride produced annually, the steam jet pump system consumes 1.996 tons of steam per hour, and consumes 15968 tons of steam per year, thereby causing huge waste.
Disclosure of Invention
The utility model aims to solve the technical problem that: the tail gas treatment device for producing phthalic anhydride by using the naphthalene method overcomes the defects of the prior art, has low content of phthalic anhydride in the treated tail gas, reduces the generation of dust in flue gas, saves the steam quantity, saves energy, reduces consumption and stabilizes the production of phthalic anhydride.
In order to solve the technical problem, the technical scheme of the utility model is that:
a tail gas treatment device for producing phthalic anhydride by a naphthalene method comprises a reactor, a gas cooler, a first switching condenser, a crude phthalic anhydride tank, a crude phthalic anhydride pretreatment group tank, a crude phthalic anhydride heater, a phthalic anhydride pretreatment tank, a light component tower, a pure phthalic anhydride tower, an evaporator and a residue washing tower; the phthalic anhydride pretreatment tank is sequentially communicated with a light component tower, a pure phthalic anhydride tower, an evaporator and a residue washing tower through a pipeline and a pump, the tops of the light component tower, the pure phthalic anhydride tower and the residue washing tower are respectively provided with a light component cooler, a pure phthalic anhydride cooler and an evaporative condenser, the discharge ports of the light component cooler, the pure phthalic anhydride cooler and the evaporative condenser are respectively communicated with the feed ports of a first air injection pump, a second air injection pump and a third air injection pump, the discharge ports of the first air injection pump, the second air injection pump and the third air injection pump are respectively communicated with the feed port of a second switching condenser, the second switching condenser is provided with a liquid material outlet and a gas material outlet, and the gas material outlet is communicated with an incinerator through a pipeline; the discharge ports of the pure phthalic anhydride cooler and the evaporative condenser are also communicated with each other and are respectively communicated with the feed port of the vacuum condenser, and the discharge port of the vacuum condenser is communicated with the phthalic anhydride pretreatment tank.
Preferably, three crude phthalic anhydride pretreatment tanks are arranged in series. And the crude phthalic anhydride is sent into a first crude phthalic anhydride pretreatment tank from a crude phthalic anhydride tank by a pump, and when the crude phthalic anhydride liquid level of the first pretreatment tank reaches a certain height, the crude phthalic anhydride overflows to a second pretreatment tank and sequentially overflows to a third pretreatment tank to finish the pretreatment of the crude phthalic anhydride. The pretreatment effect is ensured.
Preferably, the stripping section of the light component tower is provided with 16 layers of tower trays, and the rectifying section is provided with a packing layer with the height of 4.4 m. Used for separating low boilers in crude phthalic anhydride.
Preferably, 20 layers of trays are arranged in the pure phthalic anhydride tower, and the reflux ratio is about 0.5; pure phthalic anhydride is obtained from the top of the tower.
Preferably, a fixed tube-plate heat exchanger is arranged in the evaporative condenser. Condensing the crude phthalic anhydride gas in the residue washing tower.
Continuously feeding the high-boiling-point substance at the bottom of the pure phthalic anhydride tower into an evaporator, controlling the liquid level of the high-boiling-point substance, heating the residue by using high-pressure steam in the evaporator, feeding the phthalic anhydride steam into a residue washing tower, and returning the distillate obtained from the top of the tower into a phthalic anhydride pretreatment tank through a vacuum condenser for pretreatment again.
Preferably, a reflux device is arranged between the evaporator and the residue washing tower. The evaporator mainly has the function of heating the low residue of the pure phthalic anhydride tower for concentration, and continuously concentrating until the residue which cannot be recycled is completely concentrated. And washing the residual phthalic anhydride gaseous substances by an upper residue washing tower, and pumping the residual phthalic anhydride gaseous substances back to the phthalic anhydride pretreatment tank for pretreatment again.
Preferably, the evaporator is a vertical V =17.5m3 evaporator, H =4.8m D =2.4m evaporator, produced by Shandong Feicheng gold tower machinery Co.
Preferably, the light component cooler and the pure phthalic anhydride cooler are both coolers of type NEN F =70.5m2 h =5.5md =0.6m, NEN F =102.2m2, h =5.5m d = 0.7m; manufactured by kuta machines ltd, rich city, shandong. The evaporative condenser was a BEM F =36.5m2 h =6.0m d =0.4m type evaporative condenser, provided by topu industries (jiangsu) ltd.
Preferably, the first air jet pump, the second air jet pump and the third air jet pump are all F19098-0 air jets. Manufactured by Zhejiang Xin Longda vacuum Equipment, inc.
The three air jet pumps are respectively connected with the coolers at the tops of the light component tower, the pure phthalic anhydride tower and the residue washing tower, and gas in the light component tower, the pure phthalic anhydride tower and the residue washing tower is extracted to form negative pressure, so that material extraction, reflux and tail gas centralized treatment are performed, and the defect that tail gas is acquired by steam in the prior art is overcome.
Preferably, the first switch condenser and the second switch condenser are both RL5200.AC switch condensers. The equipment factory of the power transmission and transformation construction company in Hunan province. The condenser has large heat exchange area, and can greatly improve the recovery rate of phthalic anhydride in gas.
Preferably, the liquid outlet of the second switch condenser is communicated to a phthalic anhydride recovery tank through a pipeline and a pump. Temporarily storing the recovered phthalic anhydride.
Preferably, the feed inlet of the second switching condenser is communicated with the gas outlet of the first switching condenser. The tail gas generated in the reaction of generating phthalic anhydride in the previous step is treated to recover the residual phthalic anhydride.
Preferably, the discharge port of the incinerator is sequentially communicated with the washing tower and the chimney through pipelines. And (4) fully combusting the treated tail gas, washing the treated tail gas to reach the emission standard, and then discharging the tail gas.
Since the technical scheme is used, the beneficial effects of the utility model are that:
the utility model discloses utilize the air ejector extraction light component tower, pure phthalic anhydride tower and residue scrubbing tower in the air makes and forms the negative pressure in the tower to carry out material extraction, backward flow, collect the top of the tower tail gas simultaneously and deliver to second switching condenser, carry the burning furnace of burning after the phthalic anhydride of second switching condenser in with tail gas separates out again and burn. The treated tail gas has low content of phthalic anhydride and water, can be fully combusted in an incinerator, and reduces the generation of dust in the flue gas. Meanwhile, the use of a steam jet pump is abandoned, so that the steam quantity is saved, the energy is saved, the consumption is reduced, and the production of the phthalic anhydride is stabilized.
Drawings
Fig. 1 is a schematic structural circuit diagram of an embodiment of the present invention;
wherein, 1, a reactor; 2. a gas cooler; 3. a first switching condenser; 4. a crude phthalic anhydride tank; 5. pretreating and canning the crude phthalic anhydride; 6. a crude phthalic anhydride heater; 7. a phthalic anhydride pretreatment tank; 8. a light component column; 9. a pure phthalic anhydride tower; 10. an evaporator; 11. a residue washing tower; 12. a light component cooler; 13. a pure phthalic anhydride cooler; 14. an evaporative condenser; 15. a first air jet pump; 16. a second air jet pump; 17. a third air jet pump; 18. a second switch condenser; 19. an incinerator; 20. a vacuum condenser; 21. a washing tower; 22. and (4) a chimney.
Detailed Description
The invention is further explained below with reference to the drawings and examples.
Example one
As shown in figure 1, the utility model relates to a tail gas treatment device for producing phthalic anhydride by naphthalene method, which comprises a reactor 1, a gas cooler 2, a first switching condenser 3, a crude phthalic anhydride tank 4, a crude phthalic anhydride pretreatment group tank 5, a crude phthalic anhydride heater 6 and a phthalic anhydride pretreatment tank 7; the phthalic anhydride pretreatment tank 7 is sequentially communicated with a light component tower 8, a pure phthalic anhydride tower 9, an evaporator 10 and a residue washing tower 11 through pipelines and pumps, the tops of the light component tower 8, the pure phthalic anhydride tower 9 and the residue washing tower 11 are respectively provided with a light component cooler 12, a pure phthalic anhydride cooler 13 and an evaporative condenser 14, the discharge ports of the light component cooler 12, the pure phthalic anhydride cooler 13 and the evaporative condenser 14 are respectively communicated with the feed ports of a first air jet pump 15, a second air jet pump 16 and a third air jet pump 17, the discharge ports of the first air jet pump 15, the second air jet pump 16 and the third air jet pump 17 are respectively communicated with the feed port of a second switching condenser 18, the second switching condenser 18 is provided with a liquid material outlet and a gas material outlet, and the gas material outlet is communicated with an incinerator 19 through a pipeline; the discharge ports of the pure phthalic anhydride cooler 13 and the evaporative condenser 14 are also communicated with each other and are respectively communicated with the feed port of the vacuum condenser 20, and the discharge port of the vacuum condenser 20 is communicated with the phthalic anhydride pretreatment tank 7.
The discharge port of the incinerator 19 is connected to a washing tower 21 and a stack 22 in this order through pipes.
In actual application: the phthalic anhydride is produced by dehydrating and condensing phthalic acid and other by-products into products which are easy to separate in a rectification unit at 275 ℃. The crude phthalic anhydride obtained by the reaction is prepared from crude phthalic anhydrideThe phthalic anhydride tank 4 is temporarily stored, crude phthalic anhydride in the crude phthalic anhydride tank 4 is heated to 275 ℃ by a crude phthalic anhydride heater 6 after being pretreated by a third-stage pretreatment tank in a crude phthalic anhydride pretreatment group tank 5 and is conveyed to a phthalic anhydride pretreatment tank 7, the temperature is controlled to 275 ℃, and a stirrer is arranged to ensure better heat treatment and Na in the tank 2 CO 3 (10% Na added during pretreatment of crude phthalic anhydride) 2 CO 3 A solution for improving the stability of phthalic anhydride and polymerizing naphthoquinone, which is separated as a high boiling point component in the rectification process), and a material is transferred to the light component column 8 in the pretreatment process;
the pressure in the light component tower 8 is-95 kpa, the top of the tower is 187 ℃, the bottom of the tower is 208 ℃, a stripping section is provided with 16 layers of trays, a rectifying section is a packing layer with the height of 4.4m, the reflux ratio at the top of the tower is 100-250, phthalic anhydride is pumped into a pure phthalic anhydride tower 9 from the bottom of the tower by a pump, a light component cooler 12 is arranged at the top of the tower, gas is cooled and low-pressure steam is generated, and the low-pressure steam is pumped into a second switching condenser 18 through a first air jet pump 15;
the pressure in the pure phthalic anhydride tower 9 is-98 kpa, the tower top is 173 ℃, and the tower bottom is 214 ℃;20 layers of trays are arranged in the tower, and the reflux ratio is about 0.5; obtaining pure phthalic anhydride from the tower top, enabling the obtained pure phthalic anhydride to enter a pure phthalic anhydride intermediate tank (not shown) after being qualified, and then pumping the pure phthalic anhydride into a flaked packaging unit (not shown); a pure phthalic anhydride cooler 13 is arranged at the tower top, and cooled airflow is pumped into a second switching condenser 18 through a second air jet pump 16; the residue at the bottom of the tower is continuously sent to an evaporator 10;
continuously feeding high-boiling-point substances at the bottom of a pure phthalic anhydride tower 9 into an evaporator 10, controlling the liquid level of the high-boiling-point substances, heating residues, feeding phthalic anhydride steam into a residue washing tower 11, controlling the temperature in the residue washing tower 11 to be 184 ℃, and returning the distillate obtained from the top of the residue washing tower to a phthalic anhydride pretreatment tank 7 through a vacuum condenser 20 for pretreatment; the air flow pumps the cooled air flow to the second switching condenser 18 by the third air jet pump 17;
the second switching condenser 18 collects the air flows from the first air jet pump 15, the second air jet pump 16 and the third air jet pump 17, the condensed gas enters the incinerator 19 for incineration treatment and then is discharged, and the liquid enters a phthalic anhydride recovery tank (not shown).
It should be understood that these examples are only for illustrating the present invention and are not intended to limit the scope of the present invention. Furthermore, it should be understood that various changes or modifications can be made by those skilled in the art after reading the teachings of the present invention, and these equivalents also fall within the scope of the appended claims.
Claims (8)
1. A tail gas treatment device for producing phthalic anhydride by a naphthalene method comprises a reactor, a gas cooler, a first switching condenser, a crude phthalic anhydride tank, a crude phthalic anhydride pretreatment group tank, a crude phthalic anhydride heater, a phthalic anhydride pretreatment tank, a light component tower, a pure phthalic anhydride tower, an evaporator and a residue washing tower; the method is characterized in that: the phthalic anhydride pretreatment tank is sequentially communicated with a light component tower, a pure phthalic anhydride tower, an evaporator and a residue washing tower through a pipeline and a pump, a light component cooler, a pure phthalic anhydride cooler and an evaporative condenser are respectively arranged in the tops of the light component tower, the pure phthalic anhydride tower and the residue washing tower, discharge ports of the light component cooler, the pure phthalic anhydride cooler and the evaporative condenser are respectively communicated with feed ports of a first air jet pump, a second air jet pump and a third air jet pump, discharge ports of the first air jet pump, the second air jet pump and the third air jet pump are respectively communicated with a feed port of a second switching condenser, the second switching condenser is provided with a liquid material outlet and a gas material outlet, and the gas material outlet is communicated with the incinerator through a pipeline; and the discharge ports of the pure phthalic anhydride cooler and the evaporative condenser are also communicated with each other and are respectively communicated with the feed port of the vacuum condenser, and the discharge port of the vacuum condenser is communicated with the phthalic anhydride pretreatment tank.
2. The apparatus for treating tail gas from the production of phthalic anhydride by the naphthalene process according to claim 1, wherein: three crude phthalic anhydride pretreatment tanks are connected in series.
3. The apparatus for treating tail gas from the production of phthalic anhydride by the naphthalene process according to claim 1, wherein: the stripping section of the light component tower is provided with 16 layers of tower trays, and the rectifying section is provided with a packing layer with the height of 4.4 m; 20 layers of tower trays are arranged in the pure phthalic anhydride tower.
4. The apparatus for treating tail gas from the production of phthalic anhydride by naphthalene of claim 1, wherein: and a fixed tube-plate heat exchanger is arranged in the evaporative condenser.
5. The apparatus for treating tail gas from the production of phthalic anhydride by the naphthalene process according to claim 1, wherein: and a reflux device is arranged between the evaporator and the residue washing tower.
6. The apparatus for treating tail gas from the production of phthalic anhydride by naphthalene of claim 1, wherein: and the liquid material outlet of the second switching condenser is communicated with a phthalic anhydride recovery tank through a pipeline and a pump.
7. The apparatus for treating tail gas from the production of phthalic anhydride by naphthalene of claim 1, wherein: and the feed inlet of the second switching condenser is communicated with the gas outlet of the first switching condenser.
8. The apparatus for treating tail gas from the production of phthalic anhydride by naphthalene of claim 1, wherein: and the discharge port of the incinerator is sequentially communicated with the washing tower and the chimney through pipelines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222649659.2U CN218222388U (en) | 2022-10-08 | 2022-10-08 | Utilize tail gas processing apparatus of naphthalene method production phthalic anhydride |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222649659.2U CN218222388U (en) | 2022-10-08 | 2022-10-08 | Utilize tail gas processing apparatus of naphthalene method production phthalic anhydride |
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| CN218222388U true CN218222388U (en) | 2023-01-06 |
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| CN202222649659.2U Active CN218222388U (en) | 2022-10-08 | 2022-10-08 | Utilize tail gas processing apparatus of naphthalene method production phthalic anhydride |
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