CN220588943U - System for extracting crude phthalic anhydride from phthalic anhydride light components - Google Patents
System for extracting crude phthalic anhydride from phthalic anhydride light components Download PDFInfo
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- CN220588943U CN220588943U CN202321954433.1U CN202321954433U CN220588943U CN 220588943 U CN220588943 U CN 220588943U CN 202321954433 U CN202321954433 U CN 202321954433U CN 220588943 U CN220588943 U CN 220588943U
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- phthalic anhydride
- receiving tank
- tank
- light component
- pipe
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- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 title claims abstract description 69
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 title claims abstract description 69
- 238000001704 evaporation Methods 0.000 claims abstract description 53
- 230000008020 evaporation Effects 0.000 claims abstract description 46
- 239000000463 material Substances 0.000 claims abstract description 26
- 238000007599 discharging Methods 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000000605 extraction Methods 0.000 claims description 14
- 230000001502 supplementing effect Effects 0.000 claims description 11
- 150000008064 anhydrides Chemical class 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 239000011261 inert gas Substances 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 239000002826 coolant Substances 0.000 claims description 3
- 238000012546 transfer Methods 0.000 claims description 2
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 abstract description 26
- 239000005711 Benzoic acid Substances 0.000 abstract description 13
- 235000010233 benzoic acid Nutrition 0.000 abstract description 13
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 239000002920 hazardous waste Substances 0.000 abstract description 4
- 238000013461 design Methods 0.000 abstract description 2
- 239000007788 liquid Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 8
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 7
- 238000010992 reflux Methods 0.000 description 7
- 238000012986 modification Methods 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000002912 waste gas Substances 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000001577 simple distillation Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The application discloses a phthalic anhydride light component draws crude phthalic anhydride system, including evaporating kettle, its one side is connected with first inlet pipe, and the opposite side is connected with first discharging pipe; one side of the separating tower is connected with the evaporation kettle, the other side of the separating tower is connected with a second discharging pipe, and the second discharging pipe is respectively connected with the first receiving tank and the second receiving tank; a condenser provided at the top of the separation column; and one side of the first vacuumizing ejector is connected with the compressed air heater and the condenser respectively. This structural design is reasonable, uses through the cooperation of equipment such as evaporating kettle, knockout tower and condenser, can effectively utilize light component production benzoic acid, and the residual material in its production process also can get into the evaporating kettle again and be utilized, reduces phthalic anhydride hazardous waste and produces.
Description
Technical Field
The application relates to the technical field of chemical production, in particular to a system for extracting crude phthalic anhydride from phthalic anhydride light components.
Background
The phthalic anhydride light component is produced in the phthalic anhydride production process, and industrial naphthalene is subjected to catalytic oxidation reaction under the action of a catalyst, and is condensed subsequently to generate crude phthalic anhydride. The crude phthalic anhydride is pretreated by refining and then sequentially enters a light component tower and a product tower for separation, and the light component is generated at the top of the light component tower. The phthalic anhydride light component mainly comprises phthalic anhydride and benzoic acid, and a very small amount of maleic anhydride and other impurities, wherein the phthalic anhydride, the maleic anhydride, the benzoic acid and the like belong to combustible media, the toxicity grade belongs to moderate hazard, and the phthalic anhydride content is 80% -90%.
At present, after the phthalic anhydride light component in the domestic phthalic anhydride industry is doped into the phthalic anhydride heavy component, the phthalic anhydride heavy component is generally entrusted with qualification unit recovery and disposal, and the phthalic anhydride heavy component belongs to the dangerous class in solid waste. There are two modes of treatment for current qualified units: the method is characterized in that phthalic anhydride is recovered by simple distillation, the rest part is used as hazardous waste for incineration, and the other part is directly used for incineration, so that the incineration cost is paid, a great amount of resources are wasted, and a great amount of harmful gases such as carbon dioxide, carbon monoxide, sulfur dioxide and the like are generated in the incineration process, so that secondary environmental pollution is caused.
Disclosure of Invention
An objective of embodiments of the present application is to provide a system for extracting crude phthalic anhydride from phthalic anhydride light components, which is used for solving the problem that the environment is affected due to more hazardous waste of phthalic anhydride.
An object of an embodiment of the present application is to provide a phthalic anhydride light component extraction crude phthalic anhydride system, including:
one side of the evaporation kettle is connected with the first feeding pipe, and the other side of the evaporation kettle is connected with the first discharging pipe;
one side of the separating tower is connected with the evaporation kettle, the other side of the separating tower is connected with a second discharging pipe, and the second discharging pipe is respectively connected with the first receiving tank and the second receiving tank;
a condenser provided at the top of the separation column;
one side of the first vacuumizing ejector is connected with the compressed air heater and the condenser respectively;
and one side of the second vacuumizing ejector is connected with a pipeline between the first vacuumizing ejector and the compressed air heater, and the other side of the second vacuumizing ejector is respectively connected with the first receiving tank and the second receiving tank.
As an optional embodiment, the device further comprises a first air inlet pipe, wherein the first air inlet pipe is respectively connected with the first receiving tank, the second receiving tank and the evaporation kettle and is used for respectively inputting inert gases into the first receiving tank, the second receiving tank and the evaporation kettle.
As an alternative embodiment, a return pipe is arranged between the first receiving tank and the first feeding pipe and is used for returning the materials in the first receiving tank to the evaporation kettle.
As an alternative embodiment, the other end of the first discharging pipe is connected with a crude anhydride tank, and a conveying pump is arranged on the first discharging pipe and used for conveying residual materials in the evaporation kettle into the crude anhydride tank.
As an alternative embodiment, the first receiving tank and the second receiving tank are respectively connected with a heat tracing steam pipe and are used for heating materials in the first receiving tank and the second receiving tank.
As an alternative embodiment, a water supplementing pipe is arranged at one side of the condenser and is used for supplementing cooling medium into the condenser.
As an alternative embodiment, a stirring device is arranged in the evaporation kettle and is used for stirring raw materials in the evaporation kettle.
As an alternative embodiment, a heating coil is arranged in the evaporation kettle, and the heating coil is connected with a heating steam pipe and is used for heating materials in the evaporation kettle.
As an alternative embodiment, the heating coils are provided with a plurality of groups, and the groups of the heating coils are mutually independent.
As an alternative embodiment, the other side of the first vacuuming injector and the other side of the second vacuuming injector are respectively connected with an exhaust gas treatment device.
The beneficial effects of this application embodiment lie in:
this structural design is reasonable, through the cooperation of equipment such as evaporating kettle, knockout tower and condenser use, can effectively utilize light component production benzoic acid, and the residual material in its production process also can get into the evaporating kettle again and be utilized in, reduces phthalic anhydride hazardous waste and produces to changing waste into valuables, for the increase in production and income of enterprise, create the benefit. The whole extraction system reduces the use quantity of related equipment and the operation cost of enterprises on the basis of not affecting the extraction effect.
Drawings
FIG. 1 is a schematic diagram of the system for extracting crude phthalic anhydride from phthalic anhydride light components in the embodiment of the application.
Reference numerals:
1. a first vacuuming ejector; 2. a second vacuuming ejector; 3. a compressed air heater; 4. a condenser; 5. a separation tower; 6. an evaporation kettle; 7. a stirring device; 8. a transfer pump; 9. a first receiving tank; 10. a second receiving tank; 11. a second discharge pipe; 12. a second air inlet pipe; 13. a first air inlet pipe; 14. a heat tracing steam pipe; 15. heating the steam pipe; 16. a first feed tube; 17. a first discharge pipe; 18. a water supplementing pipe; 19. and (5) a return pipe.
Detailed Description
Various aspects and features of the present application are described herein with reference to the accompanying drawings.
It should be understood that various modifications may be made to the embodiments of the application herein. Therefore, the above description should not be taken as limiting, but merely as exemplification of the embodiments. Other modifications within the scope and spirit of this application will occur to those skilled in the art.
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the application and, together with a general description of the application given above and the detailed description of the embodiments given below, serve to explain the principles of the application.
These and other characteristics of the present application will become apparent from the following description of a preferred form of embodiment, given as a non-limiting example, with reference to the accompanying drawings.
It is also to be understood that, although the present application has been described with reference to some specific examples, those skilled in the art can certainly realize many other equivalent forms of the present application.
The foregoing and other aspects, features, and advantages of the present application will become more apparent in light of the following detailed description when taken in conjunction with the accompanying drawings.
Specific embodiments of the present application will be described hereinafter with reference to the accompanying drawings; however, it is to be understood that the disclosed embodiments are merely exemplary of the application, which can be embodied in various forms. Well-known and/or repeated functions and constructions are not described in detail to avoid obscuring the application with unnecessary or excessive detail. Therefore, specific structural and functional details disclosed herein are not intended to be limiting, but merely serve as a basis for the claims and as a representative basis for teaching one skilled in the art to variously employ the present application in virtually any appropriately detailed structure.
The specification may use the word "in one embodiment," "in another embodiment," "in yet another embodiment," or "in other embodiments," which may each refer to one or more of the same or different embodiments as per the application.
An object of an embodiment of the present application is to provide a phthalic anhydride light component extraction crude phthalic anhydride system, as shown in fig. 1, which includes an evaporation kettle 6, a separation tower 5, a condenser 4, a first vacuuming ejector 1 and a second vacuuming ejector 2.
One side of the evaporation kettle 6 is connected with a first feeding pipe 16, and the other side is connected with a first discharging pipe 17. As an alternative embodiment, the evaporation kettle 6 is provided with a stirring device 7 for stirring the materials in the evaporation kettle 6. The evaporation kettle 6 is internally provided with a heating coil, and the heating coil is connected with a heating steam pipe 15 and is used for heating materials in the evaporation kettle 6. The heating coils are arranged in a plurality of groups, and the heating coils are mutually independent.
Through the cooperation of agitating unit 7 and heating coil, can accelerate heating rate, reduce steam energy consumption. Moreover, when a group of heating coils leak, the heating coils can be cut out independently, stop treatment is not needed, the influence on the working efficiency is avoided, and the operation and the use of other heating coils are not influenced when the fault heating coils are cut out.
The first feeding pipe 16 is connected with a light component slag discharge tank in the refining process of the phthalic anhydride device, and light components are conveyed in the first feeding pipe 16. The other end of the first discharging pipe 17 is connected with a crude anhydride tank of the phthalic anhydride device in the oxidation process, and a conveying pump 8 is arranged on the first discharging pipe 17 and used for conveying residual materials in the evaporation kettle 6 into the crude anhydride tank. The first discharge pipe 17 is internally provided with crude phthalic anhydride.
One side of the separation tower 5 is connected with the evaporation kettle 6, the other side of the separation tower is connected with a second discharging pipe 11, and the second discharging pipe 11 is respectively connected with the first receiving tank 9 and the second receiving tank 10. Wherein the first receiving tank 9 stores middle distillate and the second receiving tank 10 stores benzoic acid.
The second discharging pipe 11 is provided with an automatic control valve for controlling the extraction quantity. Be equipped with flowmeter, sight glass on the second discharging pipe 11 and detect the volume of gathering, second discharging pipe 11 one end downwardly extending back respectively with second accepting tank 10 and first accepting tank 9 are connected, and the height of the part of second discharging pipe 11 that does not downwardly extending is higher than second accepting tank 10 and first accepting tank 9, and the distance that exceeds is not less than 10 meters, guarantees that the material of gathering flows to in the first accepting tank or in the second accepting tank 10.
As an alternative embodiment, a return pipe 19 is arranged between the first receiving tank 9 and the first feeding pipe 16, and is used for returning the material in the first receiving tank 9 to the evaporation kettle 6. The first receiving tank 9 and the second receiving tank 10 are respectively connected with a heat tracing steam pipe 14 and are used for heating materials in the first receiving tank 9 and the second receiving tank 10, and the temperature of the materials is ensured to be higher than a crystallization point, so that the materials are in a liquid state.
The first receiving tank 9 and the second receiving tank 10 are both in a negative pressure state through the second vacuumizing ejector 2 during operation, materials extracted from the separating tower 5 can enter the first receiving tank 9 or the second receiving tank 10 without cooling, and after the period is finished, the materials extracted from the first receiving tank 9 are directly pressed into the evaporating kettle 6, so that the steam consumption is low.
The condenser 4 is arranged at the top of the separation tower 5. As an alternative embodiment, a water supplementing pipe 18 is provided at one side of the condenser 4, for supplementing the cooling medium into the condenser 4. The condenser 4 is provided with a liquid level meter, the water supplementing pipe 18 is provided with a water supplementing automatic control valve, and the liquid level meter and the water supplementing automatic control valve are automatically controlled.
The maleic anhydride receiving tank is not needed, and deoxygenated water at 135 ℃ is introduced into the condenser 4 to control the temperature of the top of the separation tower 5, so that the temperature of the top of the tower is higher than the boiling point of maleic anhydride, and maleic anhydride gas enters a pipeline for vacuumizing waste gas and is then conveyed into a waste gas treatment device of the phthalic anhydride device.
The condenser 4 is filled with deoxygenated water at 135 ℃ through a water supplementing pipe 18, and the liquid level of the condenser 4 is controlled to realize the control of the temperature at the top of the tower. The method ensures that the equipment investment is low, the energy consumption is low, and a desalination water temperature water tank and a warm water circulating pump do not need to be independently arranged to form a loop and other systems.
One side of the first vacuuming ejector 1 is connected with a compressed air heater 3 and a condenser 4 respectively. One side of the compressed air heater 3 is connected with a second air inlet pipe 12, and compressed air is arranged in the second air inlet pipe 12. The compressed air heater 3 heats the compressed air to above 140 ℃, the temperature is high, the volume is large, the compressed air quantity is reduced, the energy consumption is low, and the temperature is ensured to be higher than the crystallization point of phthalic anhydride.
One side of the second vacuuming injector 2 is connected with a pipeline between the first vacuuming injector 1 and the compressed air heater 3, and the other side is respectively connected with the first receiving tank 9 and the second receiving tank 10. The other side of the first vacuuming injector 1 and the other side of the second vacuuming injector 2 are respectively connected with an exhaust gas treatment device.
The first vacuum ejector 1 controls the air amount through an automatic control valve to automatically control the pressure of the separation column 5. The second vacuum ejector 2 controls the air amount through an automatic control valve to automatically control the pressures of the first receiving tank 9 and the second receiving tank 10.
The utility model adopts the compressed air after heating to enter the other side of the first vacuumizing ejector 1 or the second vacuumizing ejector 2 for vacuumizing, has high automation degree and easy control of vacuum, and does not affect the system for extracting crude phthalic anhydride from light components of phthalic anhydride by entering the gas containing maleic anhydride extracted by the first vacuumizing ejector 1 into the waste gas treatment device (phthalic anhydride tail gas treatment device).
As an alternative embodiment, the system for extracting crude phthalic anhydride from light components of phthalic anhydride further includes a first air inlet pipe 13, where the first air inlet pipe 13 is connected to the first receiving tank 9, the second receiving tank 10 and the evaporation tank 6, respectively, and is used for inputting inert gases into the first receiving tank 9, the second receiving tank 10 and the evaporation tank 6, respectively. The inert gas in this embodiment is nitrogen.
In this embodiment, the first receiving tank 9, the second receiving tank 10 and the evaporation tank 6 are provided with pressure, temperature and liquid level detecting means, respectively. The automatic control valve, the liquid level, the pressure and the like in the embodiment are monitored by the DCS, and the automatic control valve is automatically and chemically controlled without personnel operation.
The raw materials in the first feeding pipe 16 come from a light component slag discharge tank of a phthalic anhydride device refining process, and the main components are phthalic anhydride and benzoic acid.
When the light component in the light component slag discharge tank reaches a certain liquid level, nitrogen is introduced, a feeding valve of the evaporation kettle 6 is opened, the light component is pressed into the evaporation kettle 6 through a first feeding pipe 16 for a plurality of times, rectification is started after the liquid level in the evaporation kettle 6 reaches the requirement, namely, when materials pass through a heating coil of the evaporation kettle 6, the first vacuumizing ejector 1 and the stirring device 7 are started, and the first vacuumizing ejector 1 enables the top pressure of the separation tower 5 to be maintained at-0.085 Mpa (G). 6.0Mpa (G) steam is introduced into the heating coil through an automatic control valve on the heating steam pipe 15 to heat the material in the evaporation kettle 6.
Gradually extracting benzoic acid when reflux exists at the top of the tower along with the rise of the temperature of the tower; as the kettle temperature of the post-evaporation kettle 6 increases, the benzoic acid content decreases and the phthalic anhydride content increases. When the concentration of phthalic anhydride in the evaporation kettle 6 reaches 95%, the operation is stopped, and the crude phthalic anhydride in the kettle is conveyed to a crude anhydride tank through a first discharging pipe 17 and a conveying pump 8.
The method comprises the following steps: the condenser 4 is filled with water through the water supplementing pipe 18, a certain liquid level is controlled, the temperature change of the top of the separation tower 5 is observed, when the reflux appears at the top of the tower, the first stage total reflux is firstly carried out, the outlet temperature of the condenser 4 is controlled to be more than 140 ℃, the vacuum degree is controlled to be more than-0.090 Mpa (G), the total reflux operation is carried out, low boiling point materials such as maleic anhydride and the like are conveyed to the waste gas treatment device of the phthalic anhydride device through vacuum during the total reflux operation, and then the reflux sampling analysis is carried out, at the moment, the second vacuumizing ejector 2 keeps the first receiving tank 9 and the second receiving tank 10 in a micro-negative pressure state, when the benzoic acid concentration is more than 90%, the materials are firstly extracted into the second receiving tank 10, and the extracted benzoic acid can be directly sold out as a resin raw material. When the concentration of benzoic acid is less than 90%, the middle distillate is firstly extracted to the first receiving tank 9, and as the middle distillate is continuously extracted from the top of the tower, the temperature in the kettle, the temperature at the bottom of the tower, the temperature at the middle lower point of the tower, the temperature at the upper point of the tower and the temperature at the top of the tower are sequentially increased.
When the temperature of the evaporation kettle 6 reaches the boiling point (227-233 ℃) of phthalic anhydride under vacuum at the moment, the benzoic acid content in the kettle is smaller, when the benzoic acid content at the top of the test analysis tower is less than 5%, the middle distillate extraction is finished, the total reflux of the top of the test analysis tower is finished, an automatic control valve on a heating steam pipe 15 is closed, a vacuum system is stopped, nitrogen is introduced through a first air inlet pipe 13 to break vacuum, and the first vacuumizing ejector 1 is gradually closed.
After the vacuum is eliminated, a conveying pump 8 is started, the crude phthalic anhydride in the evaporation kettle 6 is slowly pumped into a phthalic anhydride device oxidation procedure crude anhydride tank through a first discharging pipe 17 to be mixed, then the mixture enters into a refined production finished phthalic anhydride, and the rectification separation operation of one period is finished. When no crude anhydride exists in the evaporation kettle 6, the first receiving tank 9 presses nitrogen into the evaporation kettle through the first air inlet pipe 13, so that materials in the first receiving tank 9 enter the evaporation kettle 6 to be separated from light components in the next cycle, and the materials are sequentially circulated.
The above embodiments are only exemplary embodiments of the present application and are not intended to limit the present application, the scope of which is defined by the claims. Various modifications and equivalent arrangements may be made to the present application by those skilled in the art, which modifications and equivalents are also considered to be within the scope of the present application.
Claims (10)
1. A phthalic anhydride light component extraction crude phthalic anhydride system, comprising:
one side of the evaporation kettle is connected with the first feeding pipe, and the other side of the evaporation kettle is connected with the first discharging pipe;
one side of the separating tower is connected with the evaporation kettle, the other side of the separating tower is connected with a second discharging pipe, and the second discharging pipe is respectively connected with the first receiving tank and the second receiving tank;
a condenser provided at the top of the separation column;
one side of the first vacuumizing ejector is connected with the compressed air heater and the condenser respectively;
and one side of the second vacuumizing ejector is connected with a pipeline between the first vacuumizing ejector and the compressed air heater, and the other side of the second vacuumizing ejector is respectively connected with the first receiving tank and the second receiving tank.
2. The phthalic anhydride light component extraction crude phthalic anhydride system of claim 1, further comprising a first air inlet pipe, wherein the first air inlet pipe is connected to the first receiving tank, the second receiving tank, and the evaporation tank, respectively, for inputting an inert gas into the first receiving tank, the second receiving tank, and the evaporation tank, respectively.
3. The phthalic anhydride light component extraction crude phthalic anhydride system of claim 1, wherein a return line is provided between the first receiving tank and the first feed line for returning material in the first receiving tank to the evaporator.
4. The phthalic anhydride light component extraction crude phthalic anhydride system of claim 1, wherein the other end of the first discharge pipe is connected to a crude anhydride tank, and a transfer pump is provided on the first discharge pipe for transferring residual materials in the evaporation kettle to the crude anhydride tank.
5. The phthalic anhydride light component extraction crude system of claim 1, wherein the first receiving tank and the second receiving tank are each coupled to a heat trace steam line for heating the material in the first receiving tank and the second receiving tank.
6. The system for extracting crude phthalic anhydride from light components of claim 1, wherein a water make-up pipe is provided on one side of the condenser for supplementing cooling medium into the condenser.
7. The system for extracting crude phthalic anhydride from light components of claim 1, wherein a stirring device is provided in the evaporation tank for stirring the raw materials in the evaporation tank.
8. The phthalic anhydride light component extraction crude phthalic anhydride system of claim 1, wherein a heating coil is disposed in the evaporation tank, and the heating coil is connected to a heating steam pipe for heating the material in the evaporation tank.
9. The phthalic anhydride light component extraction crude phthalic anhydride system of claim 8, wherein the heating coils are configured in multiple groups, and wherein the multiple groups of heating coils are independent of each other.
10. The phthalic anhydride light component extraction crude system of claim 1, wherein the other side of the first vacuumized ejector and the other side of the second vacuumized ejector are each connected to an exhaust gas treatment device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321954433.1U CN220588943U (en) | 2023-07-24 | 2023-07-24 | System for extracting crude phthalic anhydride from phthalic anhydride light components |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321954433.1U CN220588943U (en) | 2023-07-24 | 2023-07-24 | System for extracting crude phthalic anhydride from phthalic anhydride light components |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220588943U true CN220588943U (en) | 2024-03-15 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321954433.1U Active CN220588943U (en) | 2023-07-24 | 2023-07-24 | System for extracting crude phthalic anhydride from phthalic anhydride light components |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220588943U (en) |
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2023
- 2023-07-24 CN CN202321954433.1U patent/CN220588943U/en active Active
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