CN220047112U - Diamino maleonitrile reaction solvent low temperature evaporation recovery system - Google Patents
Diamino maleonitrile reaction solvent low temperature evaporation recovery system Download PDFInfo
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- CN220047112U CN220047112U CN202321515682.0U CN202321515682U CN220047112U CN 220047112 U CN220047112 U CN 220047112U CN 202321515682 U CN202321515682 U CN 202321515682U CN 220047112 U CN220047112 U CN 220047112U
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- flash evaporation
- evaporator
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- reaction solvent
- crystallization
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- 238000001704 evaporation Methods 0.000 title claims abstract description 95
- 230000008020 evaporation Effects 0.000 title claims abstract description 94
- 239000007810 chemical reaction solvent Substances 0.000 title claims abstract description 40
- 238000011084 recovery Methods 0.000 title claims abstract description 39
- DPZSNGJNFHWQDC-ARJAWSKDSA-N (z)-2,3-diaminobut-2-enedinitrile Chemical compound N#CC(/N)=C(/N)C#N DPZSNGJNFHWQDC-ARJAWSKDSA-N 0.000 title claims abstract description 23
- 238000002425 crystallisation Methods 0.000 claims abstract description 51
- 230000008025 crystallization Effects 0.000 claims abstract description 51
- 239000002904 solvent Substances 0.000 claims abstract description 26
- 238000000034 method Methods 0.000 claims abstract description 18
- 238000007790 scraping Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 239000000463 material Substances 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 12
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 claims description 8
- 239000012295 chemical reaction liquid Substances 0.000 claims description 4
- 238000007255 decyanation reaction Methods 0.000 claims description 4
- 238000006116 polymerization reaction Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims 1
- 238000004821 distillation Methods 0.000 abstract description 10
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 239000008235 industrial water Substances 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 239000002699 waste material Substances 0.000 description 5
- 238000007333 cyanation reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 230000007547 defect Effects 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of diaminomaleonitrile reaction solvents, and discloses a low-temperature evaporation recovery system of a diaminomaleonitrile reaction solvent, which comprises a flash evaporation evaporator, wherein a flash evaporation mechanism is arranged in the flash evaporation evaporator, and the top of the flash evaporation evaporator is in an inverted cone shape; the flash evaporation mechanism comprises a motor, a rotating rod, a connecting rod and a scraping plate, wherein the motor is connected with the flash evaporation device, an output rod of the motor is connected with the rotating rod, the rotating rod is connected with the connecting rod, and the connecting rod is connected with the scraping plate. The method has the advantages that the diaminomaleonitrile reaction solvent with thermal instability is recovered by adopting a flash evaporation mechanism in a flash evaporation mode, the reaction solvent can be separated out at a lower temperature, the industrial water added in the crystallization process of the crystallization kettle is reduced under the condition of not reducing the product yield, the amount of crystallization centrifugate is further reduced, the amount of the crystallization centrifugate treated by a distillation recovery solvent system is reduced, and the treatment capacity of distillation condensate in a wastewater treatment system is reduced.
Description
Technical Field
The utility model relates to the technical field of diaminomaleonitrile reaction solvents, in particular to a low-temperature evaporation recovery system for a diaminomaleonitrile reaction solvent.
Background
In the production of diaminomaleonitrile, the long-time heating of the cyanation reaction solution accelerates the generation of polymer, resulting in reduced yield of the target product, and the selected solvent is decomposed in a heated state to cause material loss. The process system adopts the steps that process water in a crystallization kettle enters cyanide reaction liquid, diaminomaleonitrile is obtained through cooling crystallization and centrifugation, the centrifugated mother liquid enters a distillation recovery system to recover reaction solvent, and the distilled condensate is treated and discharged by a wastewater treatment system. The waste water of the cyanidation reaction crystallization is large in the production process, the crystallization time is long, and the energy consumption is high; the crystallization centrifugate is fed into the distillation recovery system to consume energy in a large amount of distillation treatment capacity, and simultaneously, the amount of the generated condensation waste water is large, the three wastes are treated in a large amount, so that the energy-saving and environment-friendly pressure of the production system is increased.
In order to overcome the defects, a reaction solvent low-temperature evaporation recovery system is combined with a crystallization device to improve the product yield, reduce the production energy consumption and reduce the wastewater production. The core is that a reaction solvent low-temperature evaporation recovery system is added, after the solvent is recovered, materials enter crystallization equipment under the condition of keeping fluidity, and the water consumption for dilution and crystallization is reduced, so that the dissolved product amount in crystallization wastewater is reduced.
Disclosure of Invention
The utility model aims to provide a low-temperature evaporation recovery system for a diaminomaleonitrile reaction solvent, which is used for solving the problems in the background art.
In order to achieve the above purpose, the present utility model provides the following technical solutions: the low-temperature evaporation recovery system for the diaminomaleonitrile reaction solvent comprises a flash evaporation evaporator, wherein a flash evaporation mechanism is arranged in the flash evaporation evaporator, and the top of the flash evaporation evaporator is in an inverted cone shape;
the flash evaporation mechanism comprises a motor, a rotating rod, a connecting rod and a scraping plate, wherein the motor is connected with the flash evaporation evaporator, an output rod of the motor is connected with the rotating rod, the rotating rod is connected with the connecting rod, the connecting rod is connected with the scraping plate, the scraping plate side scrapes the inner wall of the flash evaporation evaporator, a temperature controller is arranged in the flash evaporation evaporator, a jacket is connected to the surface of the flash evaporation evaporator, a hot water inlet pipe of the jacket is connected to the jacket, the temperature in the hot water inlet pipe of the jacket is controlled to be about 80 ℃, and the temperature in the flash evaporation evaporator is controlled through a jacket clamp.
Preferably, the left side of the flash evaporation evaporator is connected with a cyanide reactant feed pipe, the cyanide reactant feed pipe continuously flows the cyanide reactant into the flash evaporation evaporator in a certain vacuum state, the internal temperature of the flash evaporation evaporator is lower than 60 ℃ to evaporate the reaction solvent, the bottom of the flash evaporation evaporator is connected with a flash evaporation heavy phase receiving tank, and the reaction heavy phase liquid in the flash evaporation evaporator enters the flash evaporation heavy phase receiving tank.
Preferably, the flash evaporation heavy phase receiving tank is connected with a first material transferring pump, the first material transferring pump is connected with a connecting pipe, the bottom surface of the connecting pipe is connected with a crystallization kettle, the flash evaporation heavy phase receiving tank enters the crystallization kettle through the first material transferring pump, and materials in the flash evaporation heavy phase receiving tank are conveniently transferred into the crystallization kettle through the first material transferring pump.
Preferably, the crystallization kettle is connected with a process water inlet pipe, the bottom surface of the crystallization kettle is connected with a discharge pipe, the process water inlet pipe is added into the crystallization kettle to be stirred, cooled and crystallized, and after the crystallization in the crystallization kettle is completed, the crystallization liquid is subjected to solid-liquid separation treatment.
Preferably, the top surface of the flash evaporation evaporator is connected with a reaction solvent steam pipe, the reaction solvent steam pipe is connected with a condenser, the right side of the condenser is connected with a vacuum system through a vacuum connecting pipe, and solvent steam generated by distillation in the flash evaporation evaporator is led into the condenser through the reaction solvent steam pipe and then condensed and recovered.
Preferably, the bottom surface of the condenser is connected with a recovery solvent receiving tank, and the recovery solvent in the recovery solvent receiving tank is recycled to the polymerization reaction kettle for preparing reaction solvent, and meanwhile, the utilization rate of the recovery solvent is improved.
Preferably, the bottom of the recovery solvent receiving tank is connected with a second transfer pump, and the top surface of the second transfer pump is connected with a decyanation reaction batching pipe.
Compared with the prior art, the utility model has the beneficial effects that: according to the low-temperature evaporation recovery system for the diaminomaleonitrile reaction solvent, the diaminomaleonitrile reaction solvent with thermal instability is recovered by a flash evaporation mechanism in a flash evaporation mode, so that the reaction solvent can be separated out at a lower temperature, the industrial water added in the crystallization process of a crystallization kettle is reduced under the condition that the product yield is not reduced, the amount of crystallization centrifugate is further reduced, the amount of crystallization centrifugate treated by a distillation recovery solvent system is reduced, and the treatment amount of distillation condensate in a wastewater treatment system is reduced; by adopting the low-temperature evaporation recovery system of the diaminomaleonitrile reaction solvent, the waste water amount can be reduced by 80 percent, the energy consumption of the crystallization waste liquid recovery system is reduced in a same ratio, the three wastes are simultaneously reduced, the defects of the original production system are overcome under the condition of maintaining the product yield, and the purposes of improving the process system level, saving energy, reducing consumption and protecting environment are achieved.
Drawings
FIG. 1 is a schematic diagram of the overall structure connection of the present utility model;
FIG. 2 is a schematic diagram of a flash evaporator connection of the present utility model.
In the figure: the flash evaporation device comprises a flash evaporation device 1, a flash evaporation mechanism 2, a motor 201, a rotating rod 202, a connecting rod 203, a scraping plate 204, a jacket 205, a jacket hot water inlet pipe 206, a temperature controller 207, a flash evaporation heavy phase receiving tank 3, a first material transferring pump 4, a connecting pipe 5, a crystallization kettle 6, a process water inlet pipe 7, a discharge pipe 8, a reaction solvent steam pipe 9, a condenser 10, a vacuum system connecting pipe 11, a recovery solvent receiving tank 12, a second material transferring pump 13, a decyanation reaction material distributing pipe 14 and a cyanidation reaction material feeding pipe 15.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1-2, the present utility model provides a technical solution: the low-temperature evaporation recovery system for the diaminomaleonitrile reaction solvent comprises a flash evaporation evaporator 1, wherein a flash evaporation mechanism 2 is arranged in the flash evaporation evaporator 1, and the top of the flash evaporation evaporator 1 is in an inverted cone shape;
the flash evaporation mechanism 2 comprises a motor 201, a rotating rod 202, a connecting rod 203 and a scraping plate 204, wherein the motor 201 is connected with the flash evaporation evaporator 1, an output rod of the motor 201 is connected with the rotating rod 202, the rotating rod 202 is connected with the connecting rod 203, the connecting rod 203 is connected with the scraping plate 204, the side surface of the scraping plate 204 scrapes the inner wall of the flash evaporation evaporator 1, a temperature controller 207 is arranged in the flash evaporation evaporator 1, a jacket 205 is connected to the surface of the flash evaporation evaporator 1, the jacket 205 is connected with a jacket hot water inlet pipe 206, the temperature in the jacket hot water inlet pipe 206 is controlled to be about 80 ℃, and the flash evaporation mechanism 2 is used for carrying out the flash evaporation; the left side of the flash evaporation evaporator 1 is connected with a cyanation reaction material feeding pipe 15, the cyanation reaction liquid continuously flows into the flash evaporation evaporator 1 under a certain vacuum state through the cyanation reaction material feeding pipe 15, the internal temperature of the flash evaporation evaporator 1 is lower than 60 ℃ to evaporate solvent, the bottom of the flash evaporation evaporator 1 is connected with a flash evaporation heavy phase receiving tank 3, the reaction heavy phase liquid in the flash evaporation evaporator 1 enters the flash evaporation heavy phase receiving tank 3, the flash evaporation heavy phase receiving tank 3 is connected with a first transfer pump 4, the first transfer pump 4 is connected with a connecting pipe 5, the bottom surface of the connecting pipe 5 is connected with a crystallization kettle 6, the flash evaporation heavy phase receiving tank 3 enters the crystallization kettle 6 through the first transfer pump 4, the crystallization kettle 6 is connected with a process water inlet pipe 7, the bottom surface of the crystallization kettle 6 is connected with a discharge pipe 8, the process water inlet pipe 7 is added into the crystallization kettle 6 to be stirred and cooled for crystallization, after the crystallization in the crystallization kettle 6 is completed, the crystallization liquid is subjected to solid-liquid separation treatment, the top surface of the flash evaporation evaporator 1 is connected with a reaction solvent steam pipe 9, the reaction solvent steam pipe 9 is connected with a condenser 10, solvent steam generated by distillation in the flash evaporation evaporator 1 is led into the condenser 10 through the reaction solvent steam pipe 9 and then condensed and recovered, the right side of the condenser 10 is connected with a vacuum system connecting pipe 11, the bottom surface of the condenser 10 is connected with a recovery solvent receiving tank 12, the recovery solvent in the recovery solvent receiving tank 12 is recycled to a polymerization reaction kettle for preparing reaction solvent, the bottom of the recovery solvent receiving tank 12 is connected with a second transfer pump 13, the top surface of the second transfer pump 13 is connected with a decyanation reaction batching pipe 14, a diaminomaleonitrile reaction solvent low-temperature evaporation recovery system is adopted, the waste water amount can be reduced by 80%, the energy consumption of a crystallization waste liquid recovery system is reduced in the same proportion, and under the conditions of reducing three wastes and maintaining the product yield, solves the defects of the original production system, and achieves the purposes of improving the level of the process system, saving energy, reducing consumption and protecting environment.
When the device is used, the cyanidation reaction liquid continuously flows into the flash evaporation evaporator 1 under a certain vacuum state through the cyanidation reaction material feeding pipe 15, the solvent is evaporated under the condition that the internal temperature of the flash evaporation evaporator 1 is lower than 60 ℃, solvent vapor generated by distillation is condensed and recovered through the condenser 10, the recovered solvent is used for preparing reaction solvent in a polymerization reaction kettle, the reaction heavy phase liquid enters the flash evaporation heavy phase receiving tank 3, the reaction heavy phase liquid enters the crystallization kettle 6 through the first transfer pump 4, process water is added into the crystallization kettle 6 through the process water inlet pipe 7, the temperature is reduced and crystallized, after crystallization is completed, the crystallization liquid is subjected to solid-liquid separation treatment, the filtrate is distilled and recovered in the next procedure, the recovered solvent is recycled for the cyanidation reaction preparation, and meanwhile, the distilled condensed water liquid is treated by the wastewater treatment system.
Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The low-temperature evaporation recovery system for the diaminomaleonitrile reaction solvent comprises a flash evaporator (1) and is characterized in that: a flash evaporation mechanism (2) is arranged in the flash evaporation evaporator (1), and the top of the flash evaporation evaporator (1) is in an inverted cone shape;
the flash evaporation mechanism (2) comprises a motor (201), a rotating rod (202), a connecting rod (203) and a scraping plate (204), wherein the motor (201) is connected with the flash evaporation evaporator (1), an output rod of the motor (201) is connected with the rotating rod (202), the rotating rod (202) is connected with the connecting rod (203), the connecting rod (203) is connected with the scraping plate (204), the side surface of the scraping plate (204) scrapes the inner wall of the flash evaporation evaporator (1), a temperature controller (207) is arranged inside the flash evaporation evaporator (1), a jacket (205) is connected to the surface of the flash evaporation evaporator (1), a jacket hot water inlet pipe (206) is connected to the jacket hot water inlet pipe (206), and the inner temperature of the jacket hot water inlet pipe (206) is controlled at about 80 ℃.
2. The diaminomaleonitrile reaction solvent cryogenic vapor recovery system as defined in claim 1, wherein: the novel cyanide reaction kettle is characterized in that a cyanide reaction material feeding pipe (15) is connected to the left side of the flash evaporation evaporator (1), cyanide reaction liquid continuously flows into the flash evaporation evaporator (1) in a certain vacuum state through the cyanide reaction material feeding pipe (15), the internal temperature of the flash evaporation evaporator (1) is lower than 60 ℃ for evaporating solvent, the bottom of the flash evaporation evaporator (1) and a flash evaporation heavy phase receiving tank (3), and the reaction heavy phase liquid in the flash evaporation evaporator (1) enters the flash evaporation heavy phase receiving tank (3).
3. The diaminomaleonitrile reaction solvent cryogenic vapor recovery system as defined in claim 2, wherein: the flash evaporation heavy phase receiving tank (3) is connected with the first material transferring pump (4), the first material transferring pump (4) is connected with the connecting pipe (5), the bottom surface of the connecting pipe (5) is connected with the crystallization kettle (6), and the flash evaporation heavy phase receiving tank (3) enters the crystallization kettle (6) through the first material transferring pump (4).
4. A diaminomaleonitrile reaction solvent cryogenic vapor recovery system in accordance with claim 3, wherein: the crystallization kettle (6) is connected with a process water inlet pipe (7), the bottom surface of the crystallization kettle (6) is connected with a discharge pipe (8), process water is added into the crystallization kettle (6) through the process water inlet pipe (7), the temperature is reduced and crystallization is carried out through stirring, and after the crystallization in the crystallization kettle (6) is finished, the crystallization liquid is subjected to solid-liquid separation treatment.
5. The diaminomaleonitrile reaction solvent cryogenic vapor recovery system as defined in claim 1, wherein: the top surface of the flash evaporation evaporator (1) is connected with a reaction solvent steam pipe (9), the reaction solvent steam pipe (9) is connected with a condenser (10), and the right side of the condenser (10) is connected with a vacuum system connecting pipe (11).
6. The low temperature evaporation recovery system for diaminomaleonitrile reaction solvent as defined in claim 5, wherein: the bottom surface of the condenser (10) is connected with a recovery solvent receiving tank (12), and the recovery solvent in the recovery solvent receiving tank (12) is recycled to the polymerization reaction kettle for preparing reaction solvent.
7. The low temperature evaporation recovery system for diaminomaleonitrile reaction solvent as defined in claim 6, wherein: the bottom of the recovery solvent receiving tank (12) is connected with a second transfer pump (13), and the top surface of the second transfer pump (13) is connected with a decyanation reaction batching pipe (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321515682.0U CN220047112U (en) | 2023-06-14 | 2023-06-14 | Diamino maleonitrile reaction solvent low temperature evaporation recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321515682.0U CN220047112U (en) | 2023-06-14 | 2023-06-14 | Diamino maleonitrile reaction solvent low temperature evaporation recovery system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220047112U true CN220047112U (en) | 2023-11-21 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321515682.0U Active CN220047112U (en) | 2023-06-14 | 2023-06-14 | Diamino maleonitrile reaction solvent low temperature evaporation recovery system |
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| CN (1) | CN220047112U (en) |
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- 2023-06-14 CN CN202321515682.0U patent/CN220047112U/en active Active
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