Purifying device for ethyl acetate
Through the device connected in series with the three-stage evaporator and the transfer pump, high purity separation of ethyl acetate is achieved, solving the problems of high equipment costs, high energy consumption and incomplete separation in the prior art, and reducing energy consumption and acetic acid The loss of ethyl ester promotes recycling.
Patent Information
- Application Number
- CN202420497130.X
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-03-14
- Publication Date
- 2025-02-18
- Estimated Expiration
- 2034-03-14
AI Technical Summary
The existing ethyl acetate purification device has problems such as high cost of separation equipment, insufficient distillation temperature utilization, high energy consumption and incomplete separation, which affects green development.
The evaporator with three stages is sequentially connected in series to evaporate the water-containing crude ethyl acetate. The evaporators at each stage are connected through the transfer pump to achieve continuous separation of heavy components and condensation and phase separation of light components, so as to achieve high purity ethyl acetate. Separation.
The high purity (no less than 99.5%) separation of ethyl acetate is achieved, with simple process, thorough separation and low equipment investment cost, which reduces energy consumption and ethyl acetate loss and promotes recycling in chemical production.
Smart Images
Figure CN222488911U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of separation, and in particular relates to a purification device for ethyl acetate. Background Art
[0002] Ethyl acetate is low in toxicity, volatile, and can absorb water. It is a widely used fine chemical product. It can not only be used as an organic synthesis solvent for products such as petroleum, coatings, and adhesives, but can also be used as an extractant to extract organic compounds from aqueous solutions for the separation and purification of antibiotics, sugars, and biochemical products. Ethyl acetate recovery in organic synthesis production plays an important role in the recycling of solvents, reducing production costs, and improving environmental protection issues. Therefore, the purification and recovery of ethyl acetate has become a trend. The purification device of ethyl acetate in the prior art is diverse. For example, a purification device for high-purity ethyl acetate disclosed in patent CN115490594B and its purification method adopt a three-tower distillation of a distillation tower, an ethyl acetate recovery tower, and an ethanol recovery tower to purify and recover ethyl acetate and ethanol, but there are problems such as high separation equipment cost, inability to fully utilize the distillation temperature, high energy consumption, incomplete separation, and being unfavorable for green development. Utility Model Content
[0003] In order to solve the above problems, the utility model provides an ethyl acetate purification device with simple process, thorough separation, reduced ethyl acetate loss and reduced energy consumption, including an evaporator, a material transfer pump and a phase separation tank, the evaporator includes a first evaporator, a second evaporator and a third evaporator; the material transfer pump includes a first material transfer pump and a second material transfer pump; the phase separation tank includes a first phase separation tank, a second phase separation tank and a third phase separation tank; each of the evaporators is provided with a heavy component outlet and a light component outlet, the position of the heavy component outlet is lower than the position of the light component outlet; the heavy component outlet of the first evaporator is connected to the second evaporator through the first material transfer pump The inlet of the evaporator is connected; the heavy component outlet of the second evaporator is connected to the inlet of the third evaporator through the second transfer pump; the light component outlet of the first evaporator is connected to the first phase-separation tank, the light component outlet of the second evaporator is connected to the second phase-separation tank, and the light component outlet of the third evaporator is connected to the third phase-separation tank; and / or the evaporator includes an evaporation chamber, a circulation pump and a heating chamber, the outlet of the evaporation chamber is connected to the inlet of the circulation pump, the outlet of the circulation pump is connected to the inlet of the heating chamber, and the outlet of the heating chamber is connected to the inlet of the evaporation chamber.
[0004] In an optional implementation manner, the light component outlet of the second evaporator is connected to the heat medium inlet of the first evaporator, and the heat medium outlet of the first evaporator is connected to the inlet of the second phase separation tank.
[0005] In an optional implementation manner, a first condenser is connected between the first evaporator and the first phase-separation tank; and / or a second condenser is connected between the third evaporator and the third phase-separation tank.
[0006] An optional embodiment further includes a vacuum pump, and the second outlet of the first condenser, the second outlet of the second condenser, and the gas phase outlet of the second phase separation tank are all connected to the vacuum pump through a vacuum pipe.
[0007] An optional embodiment further includes a third condenser, wherein the gas phase outlet of the second phase separation tank is connected to the inlet of the third condenser, and the outlet of the third condenser is connected to the inlet of the vacuum pump.
[0008] An optional embodiment further includes a feed buffer tank, which is connected to the inlet of the first evaporator.
[0009] In an optional implementation manner, a third material transfer pump is connected between the feed buffer tank and the first evaporator.
[0010] An optional embodiment further comprises a water phase buffer tank, and the water phase outlets of the first phase separation tank, the second phase separation tank and the third phase separation tank are all connected to the inlet of the water phase buffer tank.
[0011] An optional embodiment further includes an ethyl acetate buffer tank, and the ethyl acetate outlets of the first phase separation tank, the second phase separation tank, and the third phase separation tank are connected to the inlet of the ethyl acetate buffer tank.
[0012] In an optional implementation manner, the second evaporator and the third evaporator have a heat medium inlet, and the heat medium inlet is connected to the negative pressure steam pipeline.
[0013] Compared with the prior art, the technical solution provided by the utility model has the following advantages:
[0014] The device provided by the utility model adopts three-stage evaporators connected in series in sequence to double-effect evaporate crude ethyl acetate containing water. The heavy components separated by each stage of the evaporator directly enter the next stage of the evaporator. The light components separated by the three-stage evaporator are condensed and phase-separated to directly obtain ethyl acetate with a purity of not less than 99.5%. The process is simple, the separation is thorough, and the equipment investment cost is low. The recycling of ethyl acetate is realized in chemical production, and the energy loss caused by the large reflux ratio of the distillation tower separation method is avoided. The selection of the vacuum pump enables the three-stage evaporator to evaporate under negative pressure conditions, thereby reducing the loss of ethyl acetate in the purification process. The light components of the second stage evaporator are used as the heat source of the first evaporator, further reducing the equipment investment and process energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] In order to more clearly illustrate the specific implementation methods of the utility model or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.
[0016] Figure 1 A schematic diagram of the structure of the device used in the embodiment of the present disclosure Figure 1 ;
[0017] Figure 2 A schematic diagram of the structure of the device used in the embodiment of the present disclosure Figure 2 ;
[0018] Figure 3 A schematic diagram of the structure of the device used in the embodiment of the present disclosure Figure 3 ;
[0019] Figure 4 A schematic diagram of the structure of the device used in the embodiment of the present disclosure Figure 4 ;
[0020] Figure 5 A schematic diagram of the structure of the device used in the embodiment of the present disclosure Figure 5 ;
[0021] Description of reference numerals:
[0022] Among them, 1-first evaporator, 2-first material transfer pump, 3-second evaporator, 4-second material transfer pump, 5-third evaporator, 6-first phase separation tank, 7-second phase separation tank, 8-third phase separation tank, 9-first condenser, 10-second condenser, 11-vacuum pump, 12-third condenser, 13-feed buffer tank, 14-third material transfer pump, 15-water phase buffer tank, 16-ethyl acetate buffer tank, 1-1-first heating chamber, 1-2-first circulation pump, 1-3-first evaporation chamber, 3-1-second heating chamber, 3-2-second circulation pump, 3-3-third evaporation chamber, 5-1-third heating chamber, 5-2-third circulation pump, 5-3-third evaporation chamber. DETAILED DESCRIPTION
[0023] The technical solution of the utility model will be described clearly and completely below in conjunction with the accompanying drawings. Obviously, the described embodiments are part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments of the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.
[0024] In the description of the present invention, it should be noted that the terms, "upper", "lower", "left", "right", "inner", "outer", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", and "third" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance.
[0025] In addition, the technical features involved in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.
[0026] The utility model is further described below in conjunction with the accompanying drawings and embodiments.
[0027] Please refer to Figure 1-Figure 5 The utility model provides a purification device for ethyl acetate. Example
[0028] This embodiment provides a purification device for ethyl acetate, and its structural schematic diagram is as follows Figure 1 As shown, it includes a first evaporator 1, a first material transfer pump 2, a second evaporator 3, a second material transfer pump 4, a third evaporator 5, a first phase separation tank 6, a second phase separation tank 7, and a third phase separation tank 8 which are connected in series in sequence.
[0029] Among them, the light component outlet of the first evaporator 1 is connected to the inlet of the first phase-separation tank 6, the first phase-separation tank 6 has an ethyl acetate outlet and a water phase outlet, the heavy component outlet of the first evaporator 1 is connected to the inlet of the second evaporator 3 through the first transfer pump 2, the light component outlet of the second evaporator 3 is connected to the inlet of the second phase-separation tank 7, the second phase-separation tank 7 has an ethyl acetate outlet and a water phase outlet, the heavy component outlet of the second evaporator 3 is connected to the inlet of the third evaporator 5 through the second transfer pump 4, the light component outlet of the third evaporator 5 is connected to the inlet of the third phase-separation tank 8, the third phase-separation tank 8 has an ethyl acetate outlet and a water phase outlet, and the heavy component is discharged through the heavy component outlet of the third evaporator 5.
[0030] Crude ethyl acetate enters the first evaporator 1 for evaporation, and is separated by the first evaporator 1 to obtain a light component and a heavy component. The light component enters the first phase separation tank 6 for phase separation to obtain ethyl acetate and an aqueous phase, and the heavy component is transported to the second evaporator 3 for evaporation through the first transfer pump 2. The light component in the second evaporator 3 enters the second phase separation tank 7 for phase separation to obtain ethyl acetate and an aqueous phase for the second time. The heavy component obtained for the second time is transported to the third evaporator 3 through the second transfer pump 4. The light component in the third evaporator 3 enters the third phase separation tank 8 for phase separation to obtain ethyl acetate and an aqueous phase for the third time, and the heavy component obtained for the third time is discharged from the evaporator. Example
[0031] This embodiment provides a purification device for ethyl acetate, and its structural schematic diagram is as follows Figure 2 As shown, the difference from Embodiment 1 is that this embodiment is further provided with a first condenser 9 and a second condenser 10.
[0032] On the basis of Example 1, the light component outlet of the first evaporator 1 is connected to the inlet of the first condenser 9, the first outlet of the first condenser 9 is connected to the inlet of the first phase separation tank 6, and the light component outlet of the third evaporator 5 is connected to the inlet of the second condenser 10. In order to utilize the heat energy of the evaporation process, reduce energy consumption, and improve thermodynamic efficiency, the first outlet of the second condenser 10 is connected to the inlet of the third phase separation tank 8. The light component outlet of the second evaporator 3 is connected to the heat medium inlet of the first evaporator 1, and the heat medium outlet of the first evaporator 1 is connected to the inlet of the second phase separation tank 7.
[0033] The light component and the heavy component are separated by the first evaporator 1. The light component is condensed by the first condenser 9 and enters the first phase separation tank 6 for phase separation to obtain ethyl acetate and an aqueous phase. The light component evaporated by the second evaporator 3 is used as the heat medium of the first evaporator 1, and enters the second phase separation tank 7 for phase separation to obtain ethyl acetate and an aqueous phase after heat exchange with the material in the first evaporator 1. The second heavy component obtained is evaporated by the third evaporator 5. The light component is condensed by the second condenser 10 and enters the third phase separation tank 8 for phase separation to obtain ethyl acetate and an aqueous phase for the third time. The third heavy component obtained is discharged from the evaporator. Example
[0034] This embodiment provides a purification device for ethyl acetate, and its structural schematic diagram is as follows Figure 3 As shown, the difference from Embodiment 2 is that this embodiment is further provided with a vacuum pump 11.
[0035] In order to lower the boiling point of crude ethyl acetate, reduce energy consumption, and reduce ethyl acetate loss, in this embodiment, based on Example 2, the second outlet of the first condenser 9, the second outlet of the second condenser 10, and the gas phase outlet of the second phase separation tank 7 are all connected to the vacuum pump 11 through a vacuum pipe.
[0036] The vacuum pump 11 provides a negative pressure environment for the first evaporator 1 , the second evaporator 3 and the third evaporator 5 through the first condenser 9 , the second condenser 10 and the second phase separation tank 7 . Example
[0037] This embodiment provides a purification device for ethyl acetate, and its structural schematic diagram is as follows Figure 4 As shown, the difference from Example 2 is that this embodiment is further provided with a feed buffer tank 13, a third material transfer pump 14, an aqueous phase buffer tank 15 and an ethyl acetate buffer tank 16.
[0038] On the basis of Example 2, the ethyl acetate outlets of the first phase separation tank 6, the second phase separation tank 7, and the third phase separation tank 8 are all connected to the inlet of the ethyl acetate buffer tank 16, the water phase outlets of the first phase separation tank 6, the second phase separation tank 7, and the third phase separation tank 8 are all connected to the inlet of the water phase buffer tank 15, the outlet of the feed buffer tank 13 is connected to the inlet of the first evaporator 1 through the third transfer pump 14, and the hot coal inlets of the second evaporator 3 and the third evaporator 5 are connected to the negative pressure steam pipeline.
[0039] After the crude ethyl acetate enters the feed buffer tank 13, it is transported to the first evaporator 1 through the third transfer pump 14. The ethyl acetate separated by the first phase separation tank 6, the second phase separation tank 7, and the third phase separation tank 8 enters the ethyl acetate buffer tank 16, and the water phase separated by the first phase separation tank 6, the second phase separation tank 7, and the third phase separation tank 8 enters the water phase buffer tank 15. Example
[0040] This embodiment provides a purification device for ethyl acetate, and its structural schematic diagram is as follows Figure 5 As shown, it includes a first evaporator 1, a first transfer pump 2, a second evaporator 3, a second transfer pump 4, a third evaporator 5, a first phase separation tank 6, a second phase separation tank 7, a third phase separation tank 8, a first condenser 9, a second condenser 10, a vacuum pump 11, and a third condenser 12 connected in series in sequence. The first evaporator 1, the second evaporator 3, and the third evaporator 5 have the same structure, and all include an evaporation chamber, a circulation pump, and a heating chamber. The first evaporator 1, the second evaporator 3, and the third evaporator 5 are forced circulation evaporators connected in series in sequence.
[0041] In the evaporator, the outlet of the evaporation chamber is connected to the inlet of the circulation pump, the outlet of the circulation pump is connected to the inlet of the heating chamber, the outlet of the heating chamber is connected to the inlet of the evaporation chamber, the inlet of the evaporator is located on the pipeline connecting the evaporation chamber and the circulation pump, and the heavy component outlet of the evaporator is located on the pipeline connecting the circulation pump and the heating chamber.
[0042] The light component outlet of the first evaporator 1 is connected to the inlet of the first condenser 9, the first outlet of the first condenser 9 is connected to the inlet of the first phase separation tank 6, the first phase separation tank 6 has an ethyl acetate outlet and a water phase outlet, the heavy component outlet of the first evaporator 1 is connected to the inlet of the second evaporator 3 through the first transfer pump 2, the light component outlet of the second evaporator 3 is connected to the heat medium inlet of the first heating chamber 1-3 of the first evaporator 1, the heat medium outlet of the heating chamber 1-3 of the first evaporator 1 is connected to the inlet of the second phase separation tank 7, the second phase separation tank 7 has an ethyl acetate outlet and a water phase outlet, the heavy component outlet of the second evaporator 3 is connected to the heat medium inlet of the first heating chamber 1-3 of the first evaporator 1 through the second transfer pump 4. The inlet of the third evaporator 5 is connected, the light component outlet of the third evaporator 5 is connected to the inlet of the second condenser 10, the first outlet of the second condenser 10 is connected to the inlet of the third phase separation tank 8, the third phase separation tank 8 has an ethyl acetate outlet and a water phase outlet, the second outlet of the first condenser 9 and the second outlet of the second condenser 10 are connected to the vacuum pump 11 through a vacuum pipe. In order to prevent ethyl acetate and water from entering the vacuum pump, reduce the loss of ethyl acetate, and extend the service life of the vacuum pump, the gas phase outlet of the second phase separation tank 8 is connected to the inlet of the third condenser 12, and the outlet of the third condenser 12 is connected to the vacuum pump 11 through a vacuum pipe.
[0043] The crude ethyl acetate enters the first evaporator 1, is heated in the first heating chamber 1-1, and is transported to the first evaporation chamber 1-3 by the first circulation pump 1-2 for evaporation. The light component separated by the first evaporator 1 is condensed by the first condenser 9 and then flows into the first phase separation tank 6 for phase separation to obtain ethyl acetate and an aqueous phase. The heavy component is transported to the second evaporator 3 by the first transfer pump 2. The light component separated by the second evaporator 3 is used as the heat medium of the first evaporator 1, enters the first heating chamber 1-1 of the first evaporator 1 for heat exchange with the crude ethyl acetate, and then enters the second phase separation tank 7 for phase separation for the second time to obtain ethyl acetate and an aqueous phase. The heavy component separated by the second evaporator 3 is transported to the third evaporator 5 by the second transfer pump 4 for continued evaporation. The light component separated by the third evaporator 5 is condensed by the second condenser 10 and then flows into the third phase separation tank 8 for phase separation for the third time to obtain ethyl acetate and an aqueous phase. A negative pressure environment is provided to the first evaporator 1, the second evaporator 2 and the third evaporator 3 by the vacuum pump 11 connected to the first condenser 9, the second condenser 10 and the third condenser 12.
[0044] The evaporator in the above embodiment is selected from one of a central circulation tube evaporator, a hanging basket evaporator, an external heating evaporator, a Leven evaporator, a forced circulation evaporator, a rising film evaporator, and an evaporator with direct contact heat transfer; the vacuum pump is selected from one of an oil-free vertical vacuum pump, a reciprocating vacuum pump, a water ring vacuum pump, and a Roots vacuum pump.
[0045] The above description is only a specific embodiment of the present disclosure, so that those skilled in the art can understand or implement the present disclosure. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present disclosure. Therefore, the present disclosure will not be limited to the embodiments described herein, but will conform to the widest scope consistent with the principles and novel features disclosed herein.
Claims
1. A purification device for ethyl acetate, comprising an evaporator, a material transfer pump and a phase separation tank, characterized in that: The evaporator comprises a first evaporator (1), a second evaporator (3), and a third evaporator (5); the transfer pump comprises a first transfer pump (2) and a second transfer pump (4); the phase separation tank comprises a first phase separation tank (6), a second phase separation tank (7), and a third phase separation tank (8); each evaporator is provided with a heavy component outlet and a light component outlet, and the position of the heavy component outlet is lower than the position of the light component outlet; the heavy component outlet of the first evaporator (1) is connected to the inlet of the second evaporator (3) through the first transfer pump (2); the heavy component outlet of the second evaporator (3) is connected to the inlet of the third evaporator (5) through the second transfer pump (4); the light component outlet of the first evaporator (1) is connected to the first phase separation tank (6), the light component outlet of the second evaporator (3) is connected to the second phase separation tank (7), and the light component outlet of the third evaporator (5) is connected to the third phase separation tank (8); And / or, the evaporator includes an evaporation chamber, a circulation pump and a heating chamber, the outlet of the evaporation chamber is connected to the inlet of the circulation pump, the outlet of the circulation pump is connected to the inlet of the heating chamber, and the outlet of the heating chamber is connected to the inlet of the evaporation chamber.
2. A purification device for ethyl acetate as claimed in claim 1, characterized in that: The light component outlet of the second evaporator (3) is connected to the heat medium inlet of the first evaporator (1), and the heat medium outlet of the first evaporator (1) is connected to the inlet of the second phase separation tank (7).
3. A purification device for ethyl acetate as claimed in claim 1, characterized in that: A first condenser (9) is connected between the first evaporator (1) and the first phase separation tank (6); and / or a second condenser (10) is connected between the third evaporator (5) and the third phase separation tank (8).
4. A purification device for ethyl acetate as claimed in claim 3, characterized in that: It also comprises a vacuum pump (11), and the second outlet of the first condenser (9), the second outlet of the second condenser (10), and the gas phase outlet of the second phase separation tank (7) are all connected to the vacuum pump (11) through a vacuum pipeline.
5. A purification device for ethyl acetate as claimed in claim 4, characterized in that: It also comprises a third condenser (12), the gas phase outlet of the second phase separation tank (7) is connected to the inlet of the third condenser (12), and the outlet of the third condenser (12) is connected to the inlet of the vacuum pump (11).
6. The purification device for ethyl acetate according to claim 1, characterized in that: It also comprises a feed buffer tank (13), wherein the feed buffer tank (13) is connected to the inlet of the first evaporator (1).
7. A purification device for ethyl acetate as claimed in claim 6, characterized in that: A third material transfer pump (14) is connected between the feed buffer tank (13) and the first evaporator (1).
8. The purification device for ethyl acetate according to claim 1, characterized in that: It also comprises a water phase buffer tank (15), wherein the water phase outlets of the first phase separation tank (6), the second phase separation tank (7), and the third phase separation tank (8) are all connected to the inlet of the water phase buffer tank (15).
9. A purification device for ethyl acetate as claimed in claim 8, characterized in that: It also comprises an ethyl acetate buffer tank (16), wherein the ethyl acetate outlets of the first phase separation tank (6), the second phase separation tank (7) and the third phase separation tank (8) are connected to the inlet of the ethyl acetate buffer tank (16).
10. The device for purifying ethyl acetate according to claim 9, characterized in that: The second evaporator (3) and the third evaporator (5) have a heat medium inlet, and the heat medium inlet is connected to the negative pressure steam pipeline.