CN210356589U - Maleic anhydride device solvent recovery system - Google Patents
Maleic anhydride device solvent recovery system Download PDFInfo
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- CN210356589U CN210356589U CN201921237508.8U CN201921237508U CN210356589U CN 210356589 U CN210356589 U CN 210356589U CN 201921237508 U CN201921237508 U CN 201921237508U CN 210356589 U CN210356589 U CN 210356589U
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Abstract
The utility model belongs to the technical field of maleic anhydride solvent recovery, specificly relate to a maleic anhydride device solvent recovery system. The device comprises a centrifuge, wherein a discharge port in the middle of the centrifuge is connected with a waste solvent collecting tank through a pipeline, the waste solvent collecting tank is connected with a solvent heater through a pipeline, the solvent heater is connected with a second solvent flash tank through a pipeline, and the second solvent flash tank is connected with a desorption exhaust absorption tower through a pipeline; centrifuge bottom solvent phase discharge gate passes through the pipeline and links to each other with the solvent decanter, and the solvent decanter passes through the pipeline and links to each other with the flash tank heat exchanger, and the flash tank heat exchanger passes through the pipeline and links to each other with the flash tank heater, and the flash tank heater passes through the pipeline and links to each other with first solvent flash tank. The solvent recovery system has the advantages of reasonable design, simple operation, high safety and low operation cost, reduces the loss of maleic anhydride, ensures that the treated solvent meets the requirements of technological indexes, achieves the aim of zero loss of the solvent, and ensures that the maleic anhydride device can stably operate for a long period.
Description
Technical Field
The utility model belongs to the technical field of maleic anhydride solvent recovery, specificly relate to a maleic anhydride device solvent recovery system.
Background
The maleic anhydride production process by using the n-butane oxidation solvent absorption method is a mainstream process for producing maleic anhydride at home and abroad. The process comprises the steps of generating a gas mixture containing maleic anhydride through n-butane oxidation reaction, absorbing the maleic anhydride by using a solvent, and resolving the maleic anhydride in a resolving tower. And (3) allowing one part of the resolved solvent to enter a solvent recovery unit for treatment, and directly allowing the other part of the resolved solvent to enter an absorption tower for recycling.
The following reactions mainly take place in the reactor:
main reaction:
n-C4H10+3.5O2→C4H2O3+4H2O
side reaction:
n-C4H10+4.5O2→4CO+5H2O
n-C4H10+6.5O2→4CO2+5H2O
C4H2O3+O2→4CO+H2O
C4H2O3+3O2→4CO2+H2O
n-C4H10+2.5O2→2C2H4O2+H2O
n-C4H10+3.25O2→C3H4O2+0.5CO+0.5CO2+3H2O
7C4H10+12.5O2→2C14O10+25H2O
in the recycling process of the organic solvent, a certain amount of byproducts can be accumulated, such as impurities of fumaric acid, phthalic anhydride, butanol and the like generated by pyrolysis of the solvent and hydrolysis of maleic anhydride in the solvent absorption and analysis processes, and polyacrylic acid and the like are formed by polymerization of acrylic acid. These by-products are removed by a solvent water wash section. Currently, the more organic solvent used is dibutyl phthalate (DBP). Mixing the solvent and desalted water, stirring and washing, separating the solvent phase and the water phase in a centrifuge, allowing the solvent phase to enter a solvent buffer tank or a solvent decanter to further reduce the water content in the solvent, and allowing the solvent phase to enter an absorption tower for recycling. Some intermediate phase impurities are intermittently discharged during the operation of the centrifuge, and the main components of the impurities are as follows: the solvent DBP, water, phthalic anhydride, fumaric acid, polyacrylic acid and tar (anthracene) are discharged once per hour, the discharge amount is about 40kg, sampling replacement and tail gas unit solvent recovery are added, about 60kg of waste solvent is generated per hour, 570 yuan is wasted per hour according to 9.5 yuan/kg, and about 90 yuan is increased per ton of maleic anhydride. The solvents contain more impurities, and if the solvents are not treated and enter a solvent system again, the solvents are not easy to remove by water washing, and the solvents are easy to emulsify due to impurity accumulation.
The method for treating the part of mesophase impurities in the existing device by using the solvent comprises the following steps: the wastewater is intermittently poured into a wastewater pool in small quantity, passes through a maleic anhydride sewage treatment device and is decomposed through biological treatment, so that the load and the treatment difficulty of the sewage treatment device are higher.
In addition, in the recycling process of the solvent phase organic solvent obtained by the separation of the centrifuge, a certain amount of byproducts can be accumulated, such as impurities of fumaric acid, phthalic anhydride, butanol and the like generated by the pyrolysis of the solvent and the hydrolysis of maleic anhydride in the solvent absorption and analysis processes. These by-products are not removed in time and accumulate in the solvent, which is further esterified or self-polymerized at high temperature to form a macromolecular polymer, which not only reduces the absorption efficiency, but also blocks the heat exchange equipment and causes plant downtime.
At present, dibutyl phthalate (DBP) is adopted as a more organic solvent, a series of researches are carried out in China on recycling of DBP, and the process flow is described in patent CN 2018211689115. Mixing the solvent and desalted water, stirring and washing, separating the solvent phase and the water phase in a centrifuge, reducing the water content in the solvent in a solvent buffer tank or a solvent decanter, and recycling the solvent and the desalted water in an absorption tower.
In actual operation, the water content in the solvent phase separated from the centrifuge is 2-3 wt%, which indicates that the centrifuge is in a good separation state, and after passing through a solvent buffer tank or a solvent decanter, the water content is reduced to about 1%, and the water content of the solvent still cannot reach below 0.02% of the process requirement. The poor absorption or the formation of maleic acid and fumaric acid in a system can be caused by the excessive water content of the poor solvent, the yield of maleic anhydride is reduced, and the difficulty and the loss of subsequent solvent treatment are increased.
Therefore, a novel maleic anhydride device solvent recovery system needs to be explored to recycle the organic phase and the intermediate impurity phase solvent obtained by the separation of a centrifugal machine, so that the loss of maleic anhydride is reduced, and the maleic anhydride system can stably run for a long period.
SUMMERY OF THE UTILITY MODEL
The utility model aims at overcoming the defects of the prior art and providing a solvent recovery system of a maleic anhydride device. The solvent recovery system has the advantages of reasonable design, simple operation, high safety and low operation cost, reduces the loss of maleic anhydride, ensures that the treated solvent meets the requirements of technological indexes, achieves the aim of zero loss of the solvent, and ensures that the maleic anhydride device can stably operate for a long period.
The utility model relates to a maleic anhydride device solvent recovery system, which comprises a centrifugal machine, wherein a discharge port in the middle of the centrifugal machine is connected with a waste solvent collecting tank through a pipeline, the waste solvent collecting tank is connected with a solvent heater through a pipeline, the solvent heater is connected with a second solvent flash tank through a pipeline, and the second solvent flash tank is connected with a desorption exhaust absorption tower through a pipeline; centrifuge bottom solvent phase discharge gate passes through the pipeline and links to each other with the solvent decanter, and the solvent decanter passes through the pipeline and links to each other with the flash tank heat exchanger, and the flash tank heat exchanger passes through the pipeline and links to each other with the flash tank heater, and the flash tank heater passes through the pipeline and links to each other with first solvent flash tank.
Wherein:
still include the demineralized water preheating tank, demineralized water preheating tank bottom feed inlet links to each other with the demineralized water pipeline, and the demineralized water pipeline joins the back with organic solvent feed line and links to each other with the agitator tank through first pipeline, and agitator tank bottom discharge gate passes through the pipeline and links to each other with centrifuge upper portion feed inlet.
The discharge port of the upper water phase of the centrifuge is connected with a wastewater tank through a pipeline, and the discharge port of the bottom of the wastewater tank is connected with a wastewater discharge pipeline.
The upper feed inlet of the waste solvent collecting tank is also connected with a waste solvent feed pipe.
The upper part of the solvent heater is connected with a medium-pressure steam inlet pipe.
A feed port at the upper part of the desorption and exhaust absorption tower is connected with a dry solvent feed pipe, and a discharge port at the top of the desorption and exhaust absorption tower is connected with a vacuum system through a pipeline; the bottom discharge port of the desorption exhaust absorption tower is connected with the maleic anhydride absorption tower through a pipeline.
The outlet temperature of the solvent heater is 180-195 ℃.
The absolute pressure of the second solvent flash tank was 9 mmHg.
The equipment parameters of the second solvent flash tank were as follows: diameter of
The height of the device is 2000mm, a solvent inlet DN100mm and a gas phase outlet DN150 mm.
The mass flow of the intermediate phase waste solvent discharged from the intermediate discharge port of the centrifuge is 60kg/h, and the temperature is 65 ℃.
The middle phase waste solvent discharged from the middle discharge port of the centrifuge comprises the following components: solvent DBP, water, phthalic anhydride, fumaric acid, polyacrylic acid and tar (anthracene).
The separation process of the solvent and the impurities in the waste solvent intermittently discharged from the intermediate phase of the centrifuge is as follows:
the waste intermediate phase solvent discharged intermittently by the centrifuge is discharged from a discharge port in the middle of the centrifuge, enters the waste solvent collecting tank for temporary storage through a pipeline, and further comprises a sampling replacement solvent entering through a waste solvent inlet pipe, a tail gas incineration unit cyclone separator and an incinerator bottom solvent. When the solvent in the waste solvent collecting tank reaches a certain amount, the solvent is conveyed to a solvent heater by a solvent lift pump, the upper part of the solvent heater is connected with a medium-pressure steam inlet pipe, the waste solvent is heated by the medium-pressure steam, the temperature reaches 180-plus-195 ℃, and then the waste solvent enters a second solvent flash tank through a pipeline for flash evaporation, the absolute pressure in the second solvent flash tank is 9mmHg, and the solvent is subjected to flash evaporation and recovery in a vacuum state. The flashed gas phase solvent enters the desorption exhaust absorption tower and is sprayed and absorbed by the dry solvent conveyed into the desorption exhaust absorption tower through the dry solvent feeding pipe, and the absorbed solvent is discharged from the desorption exhaust absorption tower and recycled.
The waste solvent recovery equipment intermittently discharged from the intermediate phase of the centrifuge is intermittently operated, and impurities at the bottom of the second solvent flash tank are periodically cleaned.
In the above operation, the waste solvent intermittently discharged from the centrifuge is heated and flashed under vacuum conditions to separate the solvent from impurities such as tar and polyacrylic acid, and the solvent is recovered.
For the drying process of the solvent phase obtained by the separation of the centrifuge, the following equipment is also included:
the upper part of the flash tank heater is connected with a low-pressure steam inlet pipe.
The top gas phase outlet of the first solvent flash tank is connected with a vacuum system through a pipeline, the bottom liquid phase outlet of the first solvent flash tank is connected with a flash tank heat exchanger through a dry solvent pipeline, and the flash tank heat exchanger is connected with a maleic anhydride absorption tower through a pipeline.
The mass flow of the bottom solvent phase of the centrifuge is 8000kg/h, and the temperature is 60-65 ℃.
The outlet temperature of the flash tank heat exchanger is 70-75 ℃, and the pressure is 0.38-0.42 MPa.
The outlet temperature of the flash tank heater is 95-100 ℃, and the pressure is 0.35-0.42 MPa.
The first solvent flash tank is operated at an absolute pressure of 8.5 to 9.2 mmHg.
The bottom temperature of the first solvent flash tank is 85-90 ℃.
The gas phase temperature at the top of the first solvent flash tank is 93-98 ℃.
The first solvent flash tank equipment parameters were as follows: diameter of
The height is 3000mm (no seal head is contained), the height of the filler layer is 1000mm, and the filler is positioned in the middle of the equipment; solvent inlet DN300mm, top vapor outlet DN350mm, bottom dry solvent outlet DN50 mm.
The solvent phase composition at the bottom solvent phase outlet of the centrifuge was as follows: content of solvent DBP: 98-98.5 wt%; water content: 1.5-2 wt%.
Composition of the top gas phase of the first solvent flash tank: 93-97 wt% of water and 3-7 wt% of solvent.
The composition of the dry solvent discharged from the bottom of the first solvent flash tank is: DBP content: 99-99.4 wt%; water content: less than or equal to 0.02 wt%, temperature: 76-80 ℃.
The drying and recovery process of the solvent phase discharged from the bottom of the centrifuge was as follows:
after a solvent phase discharged from the bottom of the centrifuge enters a solvent decanter, conveying the solvent to a flash tank heat exchanger by a solvent pump, and carrying out primary heat exchange with a dry solvent conveyed from a discharge port at the bottom of a first solvent flash tank through a dry solvent pipeline, wherein the outlet temperature of the flash tank heat exchanger is 70-75 ℃, and the pressure is 0.38-0.42 MPa; then the steam enters a flash tank heater, the low-pressure steam conveyed by a low-pressure steam inlet pipe is used for heating to reach the required temperature, the outlet temperature of the flash tank heater is 95-100 ℃, and the pressure is 0.35-0.42 MPa. And finally, the heated solvent phase enters a first solvent flash tank to evaporate residual moisture in the solvent, so that the moisture content in the solvent reaches 0.02% or below, and the waste gas is discharged into a vacuum system through a pipeline from a gas outlet at the top of the first solvent flash tank. The solvent after flash evaporation is conveyed by a dry solvent pump through a dry solvent pipeline, cooled by a flash tank heat exchanger and then sent back to the maleic anhydride absorption tower for recycling.
In the process, the solvent discharged from the bottom of the centrifuge is further removed, so that the process index requirement is met, the loss of maleic anhydride is reduced, and the solvent absorption and analysis system can stably run for a long period.
Through the two processes: the separation process of the solvent and impurities in the waste solvent intermittently discharged from the intermediate phase of the centrifuge and the drying and recovery process of the solvent phase discharged from the bottom of the centrifuge completely recycle the solvent in the production process of maleic anhydride, thereby realizing zero loss of the solvent.
The structure of first solvent flash tank is the same with the structure of second solvent flash tank, and the inboard top of solvent flash tank sets up the silk screen demister, and the inboard middle part sets up the packing layer, and solvent flash tank outside top sets up the gaseous phase export, and upper portion sets up the solvent import in the outside, and the outside bottom sets up the liquid phase export.
Compared with the prior art, the utility model, following beneficial effect has:
(1) maleic anhydride device solvent recovery system, centrifuge intermittent type exhaust intermediate phase waste solvent carries out recycle after the heating flash distillation, calculates according to the emission, can retrieve solvent 50Kg every hour, has not only reduced solvent loss and in the same direction as anhydride sewage treatment unit load, has also effectively reduced the processing cost, and processing cost reduces 76 yuan/ton maleic anhydride.
(2) Maleic anhydride device solvent recovery system, to centrifuge bottom exhaust solvent, the solvent drying is after the heating flash distillation, has further reduced the moisture that solvent washing workshop section brought into the absorption workshop section, has reduced the decomposition loss of maleic anhydride, has reduced the formation of impurity, guarantees that the solvent absorbs analytic system can steady long-term operation.
(3) Maleic anhydride device solvent recovery system, with the useless solvent difference recycle of the solvent phase solvent of centrifugal separation and intermittent type exhaust mesophase, system design is reasonable, easy operation, the security is high, the working costs is low, has reduced the loss of maleic anhydride, handles the back solvent and reaches the technological index requirement, has reached the purpose of zero loss of solvent, makes the maleic anhydride device can long period even running.
Drawings
FIG. 1 is a schematic diagram of a solvent recovery system for a maleic anhydride plant;
fig. 2 is a schematic structural diagram of the first solvent flash tank and the second solvent flash tank.
In the figure: 1. a stirring tank; 2. a centrifuge; 3. a solvent decanter; 4. a flash tank heat exchanger; 5. a flash tank heater; 6. A first solvent flash tank; 7. a dry solvent line; 8. a demineralized water preheating tank; 9. a desalted water line; 10. an organic solvent feed line; 11. a first pipeline; 12. a waste water tank; 13. a waste water discharge line; 14. a waste solvent collection tank; 15. a waste solvent feed pipe; 16. a solvent heater; 17. a second solvent flash tank; 18. resolving the exhaust absorption tower; 19. a dry solvent feed tube; 20. A medium pressure steam inlet pipe; 21. a low-pressure steam inlet pipe; 22. a wire mesh demister; 23. a filler layer; 24. a gas phase outlet; 25. A solvent inlet; 26. and a liquid phase outlet.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
A maleic anhydride device solvent recovery system comprises a centrifugal machine 2, wherein a discharge hole in the middle of the centrifugal machine 2 is connected with a waste solvent collecting tank 14 through a pipeline, the waste solvent collecting tank 14 is connected with a solvent heater 16 through a pipeline, the solvent heater 16 is connected with a second solvent flash tank 17 through a pipeline, and the second solvent flash tank 17 is connected with an analysis exhaust absorption tower 18 through a pipeline; the solvent phase discharge hole at the bottom of the centrifuge 2 is connected with the solvent decanter 3 through a pipeline, the solvent decanter 3 is connected with the flash tank heat exchanger 4 through a pipeline, the flash tank heat exchanger 4 is connected with the flash tank heater 5 through a pipeline, and the flash tank heater 5 is connected with the first solvent flash tank 6 through a pipeline.
Still include demineralized water preheating tank 8, 8 bottom feed inlets of demineralized water preheating tank link to each other with demineralized water pipeline 9, and demineralized water pipeline 9 joins with organic solvent feed line 10 and links to each other with agitator tank 1 through first pipeline 11 after, and 1 bottom discharge gate of agitator tank passes through the pipeline and links to each other with 2 upper portion feed inlets of centrifuge.
The upper water phase discharge port of the centrifuge 2 is connected with a waste water tank 12 through a pipeline, and the bottom discharge port of the waste water tank 12 is connected with a waste water discharge pipeline 13.
The upper feed port of the waste solvent collecting tank 14 is also connected to a waste solvent feed pipe 15.
The upper part of the solvent heater 16 is connected with a medium-pressure steam inlet pipe 20.
A feed port at the upper part of the desorption and exhaust absorption tower 18 is connected with a dry solvent feed pipe 19, and a discharge port at the top of the desorption and exhaust absorption tower 18 is connected with a vacuum system through a pipeline; the bottom discharge hole of the desorption exhaust absorption tower 18 is connected with the maleic anhydride absorption tower through a pipeline.
The outlet temperature of the solvent heater 16 was 185 ℃.
The absolute pressure of the second solvent flash tank was 9 mmHg.
The equipment parameters of the second solvent flash tank were as follows: diameter of
The height of the device is 2000mm, a solvent inlet DN100mm and a gas phase outlet DN150 mm.
The mass flow of the intermediate phase waste solvent discharged from the intermediate discharge port of the centrifuge is 60kg/h, and the temperature is 65 ℃.
The separation process of the solvent and the impurities in the waste solvent intermittently discharged from the intermediate phase of the centrifuge is as follows:
the intermediate phase waste solvent intermittently discharged by the centrifuge 2 is discharged from a discharge port in the middle of the centrifuge 2, enters the waste solvent collecting tank 14 for temporary storage through a pipeline, and the solvent entering the waste solvent collecting tank 14 for temporary storage further comprises a sampling replacement solvent entering through a waste solvent inlet pipe 15, a tail gas incineration unit cyclone separator and an incinerator bottom solvent. When the solvent in the waste solvent collecting tank 14 reaches a certain amount, the solvent is conveyed to the solvent heater 16 by the solvent lift pump, the upper part of the solvent heater 16 is connected with the medium-pressure steam inlet pipe 20, the waste solvent is heated by the medium-pressure steam, the temperature reaches 185 ℃, and then the waste solvent enters the second solvent flash tank 17 through a pipeline for flash evaporation, the absolute pressure in the second solvent flash tank 17 is 9mmHg, and the solvent is recovered by flash evaporation in a vacuum state. The flashed vapor phase solvent enters the desorption exhaust absorption tower 18 and is sprayed and absorbed by the dry solvent conveyed into the desorption exhaust absorption tower 18 through the dry solvent feeding pipe 19, and the absorbed solvent is discharged from the desorption exhaust absorption tower 18 for recycling.
Wherein: the middle phase waste solvent discharged from the middle discharge port of the centrifuge comprises the following components: solvent DBP, water, phthalic anhydride, fumaric acid, polyacrylic acid and tar (anthracene).
After the above operation, the solvent DBP is completely separated from other impurities.
The waste solvent recovery equipment intermittently discharged from the intermediate phase of the centrifuge is intermittently operated, and impurities at the bottom of the second solvent flash tank are periodically cleaned.
In the above operation, the waste solvent intermittently discharged from the centrifuge is heated and flashed under vacuum conditions to separate the solvent from impurities such as tar and polyacrylic acid, and the solvent is recovered.
For the drying process of the solvent phase obtained by the separation of the centrifuge, the following equipment is also included:
the upper part of the flash tank heater 5 is connected with a low-pressure steam inlet pipe 21.
The discharge port at the top of the first solvent flash tank 6 is connected with a vacuum system through a pipeline, the discharge port at the bottom of the first solvent flash tank 6 is connected with the flash tank heat exchanger 4 through a dry solvent pipeline 7, and the flash tank heat exchanger 4 is connected with a maleic anhydride absorption tower through a pipeline.
The outlet temperature of the flash tank heat exchanger 4 is 75 ℃, and the pressure is 0.4 MPa.
The outlet temperature of the flash tank heater 5 is 100 ℃ and the pressure is 0.39 MPa.
The first solvent flash drum 6 is operated at a pressure of 9mmHg absolute.
The bottom temperature of the first solvent flash tank 6 was 85 ℃.
The vapor temperature at the top of the first solvent flash tank 6 was 93 ℃.
The equipment parameters of the first solvent flash tank 6 are as follows: diameter of
Height 3000mm (no head), height of the filler layer: 1000mm, the filler is positioned in the middle of the equipment; solvent inlet DN300mm, top vapor outlet DN350mm, bottom dry solvent outlet DN50 mm.
The mass flow of the solvent at the bottom outlet of the centrifuge is 8000kg/h, and the temperature is 65 ℃.
The solvent phase composition at the bottom outlet of the centrifuge was as follows: the DBP content of the solvent is 98.5wt percent; the water content was 1.5 wt%.
First solvent flash tank 6 top gas phase composition: the water content was 94.49 wt%, and the solvent content was 5.51 wt%.
The composition of the dry solvent discharged from the bottom of the first solvent flash tank 6 is: DBP content: 99.4 wt%; water content: less than or equal to 0.02wt percent.
The drying and recovery process of the solvent phase discharged from the bottom of the centrifuge was as follows:
after a solvent phase discharged from the bottom of the centrifuge 2 enters the solvent decanter 3, the solvent is conveyed to a flash tank heat exchanger 4 by a solvent pump, and is subjected to primary heat exchange with a dry solvent conveyed from a bottom discharge port of a first solvent flash tank 6 through a dry solvent pipeline 7, wherein the outlet temperature of the flash tank heat exchanger 4 is 75 ℃, and the pressure is 0.4 MPa; then enters a flash tank heater 5, the low-pressure steam delivered by a low-pressure steam inlet pipe 21 is used for heating to reach the required temperature, the outlet temperature of the flash tank heater 5 is 100 ℃, and the pressure is 0.39 MPa. The heated solvent phase finally enters a first solvent flash tank 6 to evaporate residual moisture in the solvent, so that the moisture content in the solvent reaches 0.02% or below, and the waste gas is discharged into a vacuum system through a pipeline from a gas outlet at the top of the first solvent flash tank 6. The solvent after flash evaporation is conveyed by a dry solvent pump through a dry solvent pipeline 7, cooled by a flash tank heat exchanger 4 and then sent back to the maleic anhydride absorption tower for recycling.
Wherein:
the mass flow of the solvent at the bottom outlet of the centrifuge is 8000kg/h, and the temperature is 65 ℃.
The solvent phase composition at the bottom outlet of the centrifuge was as follows: the DBP content of the solvent is 98.5wt percent; the water content was 1.5 wt%.
The composition of the dry solvent discharged from the bottom of the first solvent flash tank 6 is: DBP content: 99.4 wt%; water content: less than or equal to 0.02wt percent.
The first solvent flash tank and the second solvent flash tank adopted in the two treatment processes have the same structure, the top of the inner side of the solvent flash tank is provided with a silk screen demister 22, the middle of the inner side is provided with a packing layer 23, the top of the outer side of the solvent flash tank is provided with a gas phase outlet 24, the upper middle part of the outer side is provided with a solvent inlet 25, and the bottom of the outer side is provided with a liquid phase outlet 26.
Claims (10)
1. A maleic anhydride device solvent recovery system is characterized in that: the device comprises a centrifugal machine (2), wherein a discharge hole in the middle of the centrifugal machine (2) is connected with a waste solvent collecting tank (14) through a pipeline, the waste solvent collecting tank (14) is connected with a solvent heater (16) through a pipeline, the solvent heater (16) is connected with a second solvent flash tank (17) through a pipeline, and the second solvent flash tank (17) is connected with a desorption exhaust absorption tower (18) through a pipeline; the bottom solvent phase discharge hole of the centrifuge (2) is connected with a solvent decanter (3) through a pipeline, the solvent decanter (3) is connected with a flash tank heat exchanger (4) through a pipeline, the flash tank heat exchanger (4) is connected with a flash tank heater (5) through a pipeline, and the flash tank heater (5) is connected with a first solvent flash tank (6) through a pipeline.
2. The maleic anhydride plant solvent recovery system of claim 1, wherein: still include demineralized water preheating tank (8), demineralized water preheating tank (8) bottom feed inlet links to each other with demineralized water pipeline (9), demineralized water pipeline (9) join with organic solvent feed pipeline (10) back and link to each other with agitator tank (1) through first pipeline (11), agitator tank (1) bottom discharge gate passes through the pipeline and links to each other with centrifuge (2) upper portion feed inlet, centrifuge (2) upper portion aqueous phase discharge gate passes through the pipeline and links to each other with waste water tank (12), waste water tank (12) bottom discharge gate links to each other with waste water discharge pipeline (13).
3. The maleic anhydride plant solvent recovery system of claim 1, wherein: the upper feed inlet of the waste solvent collecting tank (14) is also connected with a waste solvent feed pipe (15).
4. The maleic anhydride plant solvent recovery system of claim 1, wherein: the upper part of the solvent heater (16) is connected with a medium-pressure steam inlet pipe (20).
5. The maleic anhydride plant solvent recovery system of claim 1, wherein: a feed inlet at the upper part of the desorption and exhaust absorption tower (18) is connected with a dry solvent feed pipe (19), and a discharge outlet at the top of the desorption and exhaust absorption tower (18) is connected with a vacuum system through a pipeline; the bottom discharge hole of the desorption exhaust absorption tower (18) is connected with the maleic anhydride absorption tower through a pipeline.
6. The maleic anhydride plant solvent recovery system of claim 1, wherein: the equipment parameters of the second solvent flash tank (17) are as follows: diameter of
The height of the device is 2000mm, a solvent inlet DN100mm and a gas phase outlet DN150 mm.
7. The maleic anhydride plant solvent recovery system of claim 1, wherein: the upper part of the flash tank heater (5) is connected with a low-pressure steam inlet pipe (21).
8. The maleic anhydride plant solvent recovery system of claim 1, wherein: a gas phase outlet (24) at the top of the first solvent flash tank (6) is connected with a vacuum system through a pipeline, a liquid phase outlet (26) at the bottom of the first solvent flash tank (6) is connected with a flash tank heat exchanger (4) through a dry solvent pipeline (7), and the flash tank heat exchanger (4) is connected with a maleic anhydride absorption tower through a pipeline.
9. The maleic anhydride plant solvent recovery system of claim 1, wherein: the equipment parameters of the first solvent flash tank (6) are as follows: diameter of
Height 3000mm, packing layer height: 1000mm, the filler is positioned in the middle of the equipment; solvent inlet DN300mm, top vapor outlet DN350mm, bottom dry solvent outlet DN50 mm.
10. The maleic anhydride plant solvent recovery system of claim 1, wherein: first solvent flash tank (6) are the same with the structure of second solvent flash tank (17), and the inboard top of solvent flash tank sets up silk screen demister (22), and inboard middle part sets up packing layer (23), and solvent flash tank outside top sets up gaseous phase export (24), and upper portion sets up solvent import (25) in the outside, and the outside bottom sets up liquid phase export (26).
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| CN201921237508.8U CN210356589U (en) | 2019-07-30 | 2019-07-30 | Maleic anhydride device solvent recovery system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114100171A (en) * | 2021-11-23 | 2022-03-01 | 洛阳炼化九源石化有限公司 | Heavy oil treatment method and system for maleic anhydride production by n-butane method |
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2019
- 2019-07-30 CN CN201921237508.8U patent/CN210356589U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114100171A (en) * | 2021-11-23 | 2022-03-01 | 洛阳炼化九源石化有限公司 | Heavy oil treatment method and system for maleic anhydride production by n-butane method |
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