Separation process of ethyl acetate and butanone

Abstract

The invention belongs to the technical field of separation, and particularly relates to a separation process of ethyl acetate and butanone, which comprises the following steps: a butanone-ethyl acetate-ethanol mixture to be treated enters the middle part of a butanone separation tower, liquid produced from the top of the butanone separation tower is continuously introduced into an ethanol separation tower, and a butanone product is continuously produced from the bottom of the butanone separation tower; continuously introducing tower top produced liquid of the ethanol separation tower into an ethyl acetate separation tower, and continuously producing an ethanol product from the tower bottom of the ethanol separation tower; liquid produced from the top of the ethyl acetate separation tower returns to the butanone separation tower, and ethyl acetate products are continuously produced from the bottom of the ethyl acetate separation tower. According to the method, the ethanol is introduced as an entrainer, the azeotropic ratio of the ethanol to the ethyl acetate and the butanone is obviously changed by changing the operation pressure, and the operation is performed in different rectification areas generated under different pressure conditions, so that the operation difficulty of direct pressure swing rectification separation of the ethyl acetate and the butanone is reduced, and the separation of the ethyl acetate and the butanone is realized.

Description

Technical Field

[0001] The invention belongs to the technical field of separation, and in particular relates to a separation process of ethyl acetate and butanone. Background Art

[0002] Ethyl acetate and butanone are both commonly used organic solvents, widely used in dyes, coatings, detergents, pharmaceuticals and other industries. Ethyl acetate and butanone are azeotropic and miscible, and cannot be separated by direct distillation or pressure swing distillation.

[0003] The prior art proposes the idea of ​​using ethylene glycol, DMSO, NMP, etc. as extractants for extractive distillation to separate ethyl acetate and butanone. Although theoretical simulation calculations are feasible, it is found through practical applications that the extractants cannot achieve the expected separation effect, and ethyl acetate and butanone cannot be separated. There is currently no good solution for the separation and purification of the mixed solution of the two. Summary of the invention

[0004] In view of the above shortcomings of the prior art, the purpose of the present invention is to provide a separation process of ethyl acetate and butanone. Ethyl acetate and butanone are two substances in different distillation regions, and the azeotrope is not sensitive to pressure changes. The present invention introduces a new additive (ethanol) to form a distillation boundary line with one end sensitive to pressure changes, and then uses pressure swing distillation to separate ethyl acetate and butanone. The three components of the ethanol / ethyl acetate / butanone ternary mixture in the present invention form azeotropes between each other, and the two distillation boundary lines formed at the same time gradually approach near the ethanol / ethyl acetate azeotrope, forming a distillation boundary line clamping point. The binary azeotrope formed by ethanol / ethyl acetate is sensitive to pressure changes, and a pressure swing distillation process design method for overcoming the distillation boundary line clamping point through pressure optimization is proposed, and the separation of ethyl acetate and butanone is achieved by using a three-tower process.

[0005] To achieve the above objectives, the technical solutions adopted are: One of the purposes of the present invention is to provide a separation process of ethyl acetate and butanone, comprising the following steps: the operating pressure of a butanone separation tower is pressurized, a butanone-ethyl acetate-ethanol mixture to be treated enters the middle of the butanone separation tower, a first top produced liquid of the butanone separation tower is continuously passed into an ethanol separation tower, and a butanone product is continuously produced from the bottom of the butanone separation tower; the operating pressure of the ethanol separation tower is negative pressure, a second top produced liquid of the ethanol separation tower is continuously passed into an ethyl acetate separation tower, and an ethanol product is continuously produced from the bottom of the ethanol separation tower; the operating pressure of the ethyl acetate separation tower is normal pressure, a third top produced liquid of the ethyl acetate separation tower is returned to the butanone separation tower, and an ethyl acetate product is continuously produced from the bottom of the ethyl acetate separation tower.

[0006] Furthermore, the device for realizing the separation process of ethyl acetate and butanone mainly comprises a butanone separation tower, an ethanol separation tower and an ethyl acetate separation tower which are connected in sequence.

[0007] Furthermore, the butanone separation tower is provided with a material inlet, and a reboiler is connected to the bottom of the tower. The bottom of the ethyl acetate separation tower is connected to a second thermally coupled reboiler, the top of the butanone separation tower is connected to the second thermally coupled reboiler, the second thermally coupled reboiler is respectively connected to a first trap and a first reflux tank, the first trap is connected to the first reflux tank, the first reflux tank is connected to a first reflux pump, the first reflux pump is respectively connected to the top of the butanone separation tower and the middle of the ethanol separation tower, the bottom of the butanone separation tower is connected to a first bottom circulating material transfer pump, the first bottom circulating material transfer pump is connected to a butanone product outlet, the top of the ethanol separation tower is sequentially connected to a second trap and a second reflux tank, the second reflux tank is connected to a second reflux pump, the second reflux pump is respectively connected to the top of the ethanol separation tower and the acetic acid In the middle of the ethyl ester separation tower, the bottom of the ethanol separation tower is respectively connected with the first thermal coupling reboiler and the second bottom circulating material transfer pump, the second bottom circulating material transfer pump is respectively connected with the first thermal coupling reboiler and the ethanol product outlet, the top of the ethyl acetate separation tower is connected with the first thermal coupling reboiler, the first thermal coupling reboiler is respectively connected with the third trap and the third reflux tank, the third trap is connected with the third reflux tank, the third reflux tank is connected with the third reflux pump, the third reflux pump is respectively connected with the top of the ethyl acetate separation tower and the material inlet in the butanone separation tower, the bottom of the ethyl acetate separation tower is connected with the third bottom circulating material transfer pump, the third bottom circulating material transfer pump is respectively connected with the second thermal coupling reboiler and the ethyl acetate product outlet.

[0008] The first collector is connected to a first exhaust gas outlet, the second collector is connected to a second exhaust gas outlet, and the third collector is connected to a third exhaust gas outlet.

[0009] Further, the separation process of ethyl acetate and butanone comprises the following specific steps: The operating pressure of the butanone separation tower is pressurized, and the butanone-ethyl acetate-ethanol mixture to be treated enters the middle part of the butanone separation tower from the material inlet. Under the pressurized condition, steam is used as a heat source and indirectly heated through a reboiler. The first tower top gas phase generated after heating is used as a heat source to heat the second thermally coupled reboiler of the ethyl acetate separation tower. The obtained first heat-exchanged gas-liquid mixture is divided into two parts, one part is a first condensate, and the other part is a first uncondensed gas phase. The first uncondensed gas phase is condensed through a first trap, and the obtained first condensed liquid phase and the first condensate enter the first reflux tank together, and are forced to reflux and extract through a first reflux pump. The first reflux liquid returns to the top of the butanone separation tower, and the first tower top produced liquid is continuously passed into the middle part of the ethanol separation tower. The first tower bottom liquid of the butanone separation tower is continuously extracted with a butanone product through a first tower bottom circulation transfer pump; The operating pressure of the ethanol separation tower is negative pressure, and the heat source comes from the third tower top gas phase of the ethyl acetate separation tower, which exchanges heat with the second tower bottom liquid of the ethanol separation tower in the first thermal coupling reboiler. After the second tower bottom liquid is heated and vaporized, its gaseous mixed component, the second tower top gas phase, is condensed and cooled by the second trap, and the obtained second condensed liquid phase enters the second reflux tank and is forced to reflux and withdrawn by the second reflux pump. The obtained second reflux liquid returns to the ethanol separation tower, and the second tower top withdrawn liquid is continuously introduced into the middle part of the ethyl acetate separation tower, and the second tower bottom liquid of the ethanol separation tower is continuously withdrawn from the ethanol product by the second tower bottom circulating material transfer pump; The operating pressure of the ethyl acetate separation tower is normal pressure, and the heat source comes from the first top gas phase of the butanone separation tower. The first top gas phase and the third bottom liquid of the ethyl acetate separation tower are heat-exchanged in the second thermal coupling reboiler, and the third bottom liquid is heated and vaporized. The generated third top gas phase goes to the first thermal coupling reboiler at the bottom of the ethanol separation tower for heat exchange, and the second heat-exchanged gas-liquid mixture is divided into two parts, one part is the second condensate, and the other part is the second uncondensed gas phase. The second uncondensed gas phase is condensed into a third condensed liquid phase through a third trap, and enters the third reflux tank together with the second condensate, and is forced to reflux and extract through a third reflux pump. The third reflux liquid returns to the top of the ethyl acetate separation tower, and the third top produced liquid returns to the material inlet of the butanone separation tower. The third bottom liquid of the ethyl acetate separation tower is continuously extracted from the ethyl acetate product through the third bottom circulating material transfer pump.

[0010] Furthermore, the operating pressure of the butanone separation tower is 400-700 kPaG, the number of theoretical plates is 40-80, and the reflux ratio is 3-15.

[0011] Furthermore, the operating pressure of the ethanol separation tower is 30-70 kPaA, the number of theoretical plates is 20-60, and the reflux ratio is 1-5.

[0012] Furthermore, the ethyl acetate separation tower has a theoretical plate number of 30-80 and a reflux ratio of 2-10.

[0013] Compared with the prior art, the present invention has the following beneficial effects: The present invention provides a new process scheme for separating ethyl acetate and butanone, wherein ethanol is introduced as an azeotropic agent, and the azeotropic ratio between ethanol, ethyl acetate and butanone is significantly changed by changing the operating pressure, and different distillation regions generated under different pressure conditions are operated, thereby reducing the operational difficulty of direct pressure swing distillation to separate ethyl acetate and butanone, thereby achieving separation of the two. At the same time, heat coupling can be achieved between distillation towers with different operating pressures, thereby further reducing the energy consumption of the distillation separation process, and having high operability. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 The present invention is a process flow chart of a separation process of ethyl acetate and butanone; Figure 2 is the ternary phase diagram under normal pressure conditions; Figure 3 It is the ternary phase diagram under 600kPaA; Figure 4 It is the ternary phase diagram under 50kPaA condition; The accompanying drawings are marked as follows: 11, butanone separation tower; 12, reboiler; 13, first collector; 14, first reflux tank; 15, first bottom circulation transfer pump; 16, first reflux pump; 17, first waste gas outlet; 21, ethanol separation tower; 22, first thermally coupled reboiler; 23, second collector; 24, second reflux tank; 25, second bottom circulation transfer pump; 26, second reflux pump; 27, second waste gas outlet; 31, ethyl acetate separation tower; 32, second thermally coupled reboiler; 33, third collector; 34, third reflux tank; 35, third bottom circulation transfer pump; 36, third reflux pump; 37, third waste gas outlet; 111, butanone-ethyl acetate-ethanol mixture to be treated; 1 12. The first tower top gas phase; 113. The first liquid phase after condensation; 114. The first reflux liquid; 115. The first tower top produced liquid; 116. The first gas-liquid mixture after heat exchange; 117. The first tower bottom liquid; 118. The first uncondensed gas phase; 119. The first condensed liquid; 212. The second tower top gas phase; 213. The second liquid phase after condensation; 214. The second reflux liquid; 215. The second tower top produced liquid; 216. The second tower bottom liquid; 312. The third tower top gas phase; 313. The third liquid phase after condensation; 314. The third reflux liquid; 315. The third tower top produced liquid; 316. The second gas-liquid mixture after heat exchange; 317. The third tower bottom liquid; 318. The second uncondensed gas phase; 319. The second condensed liquid. DETAILED DESCRIPTION

[0015] The present invention is described below in conjunction with examples, which are only used to explain the present invention and are not used to limit the scope of the present invention.

[0016] Reference Figure 1 The device for implementing this process includes three sets of distillation towers, namely a butanone separation tower 11, an ethanol separation tower 21 and an ethyl acetate separation tower 31.

[0017] A material inlet is provided in the butanone separation tower 11, a reboiler 12 is connected to the bottom of the tower, a second thermally coupled reboiler 32 is connected to the bottom of the ethyl acetate separation tower 31, the top of the butanone separation tower 11 is connected to the second thermally coupled reboiler 32, the second thermally coupled reboiler 32 is respectively connected to a first trap 13 and a first reflux tank 14, the first trap 13 is connected to the first reflux tank 14, the first reflux tank 14 is connected to a first reflux pump 16, the first reflux pump 16 is respectively connected to the top of the butanone separation tower 11 and the middle of the ethanol separation tower 21, the bottom of the butanone separation tower 11 is connected to a first bottom circulating material transfer pump 15, the first bottom circulating material transfer pump 15 is connected to a butanone product outlet, the top of the ethanol separation tower 21 is sequentially connected to a second trap 23 and a second reflux tank 24, the second reflux tank 24 is connected to a second reflux pump 26, the second reflux pump 26 is respectively The top of the ethanol separation tower 21 and the middle of the ethyl acetate separation tower 31 are connected, the bottom of the ethanol separation tower 21 is respectively connected with the first thermally coupled reboiler 22 and the second bottom circulating material transfer pump 25, the second bottom circulating material transfer pump 25 is respectively connected with the first thermally coupled reboiler 22 and the ethanol product outlet, the top of the ethyl acetate separation tower 31 is connected with the first thermally coupled reboiler 22, the first thermally coupled reboiler 22 is respectively connected with the third trap 33 and the third reflux tank 34, the third trap 33 is connected with the third reflux tank 34, the third reflux tank 34 is connected with the third reflux pump 36, the third reflux pump 36 is respectively connected with the top of the ethyl acetate separation tower 31 and the material inlet in the butanone separation tower 11, the bottom of the ethyl acetate separation tower 31 is connected with the third bottom circulating material transfer pump 35, the third bottom circulating material transfer pump 35 is respectively connected with the second thermally coupled reboiler 32 and the ethyl acetate product outlet.

[0018] The first collector 13 is connected to a first exhaust gas outlet 17 , the second collector 23 is connected to a second exhaust gas outlet 27 , and the third collector 33 is connected to a third exhaust gas outlet 37 .

[0019] The operating pressure of the butanone separation tower 11 is pressurized, and the butanone-ethyl acetate-ethanol mixture 111 to be treated enters the middle of the butanone separation tower 11 from the material inlet. Under the pressurized condition, steam is used as a heat source and indirectly heated through the reboiler 12. The first tower top gas phase 112 generated after heating is used as a heat source to heat the second thermally coupled reboiler 32 of the ethyl acetate separation tower 31. The first gas-liquid mixture 116 obtained after heat exchange is divided into two parts, one part is the first condensate 119, and the other part is the first The uncondensed gas phase 118, the first uncondensed gas phase 118 is condensed by the first collector 13, and the obtained first condensed liquid phase 113 and the first condensate 119 enter the first reflux tank 14 together, and are forced to reflux and produce by the first reflux pump 16, the first reflux liquid 114 returns to the top of the butanone separation tower 11, and the first top produced liquid 115 is continuously passed into the middle part of the ethanol separation tower 21, and the first bottom liquid 117 of the butanone separation tower 11 is continuously produced by the first bottom circulation transfer pump 15 to produce butanone product.

[0020] The operating pressure of the ethanol separation tower 21 is negative pressure. The heat source of the tower comes from the third top gas phase 312 of the ethyl acetate separation tower 31, and heat is exchanged with the second bottom liquid 216 of the ethanol separation tower 21 in the first thermal coupling reboiler 22. After the second bottom liquid 216 is heated and vaporized, its gaseous mixed component, the second top gas phase 212, is condensed and cooled by the second collector 23. The obtained second condensed liquid phase 213 enters the second reflux tank 24 and is forced to reflux and withdrawn by the second reflux pump 26. The obtained second reflux liquid 214 returns to the ethanol separation tower 21, and the second top produced liquid 215 is continuously passed into the middle part of the ethyl acetate separation tower 31. The second bottom liquid 216 of the ethanol separation tower 21 is continuously withdrawn from the ethanol product by the second bottom circulation transfer pump 25.

[0021] The operating pressure of the ethyl acetate separation tower 31 is normal pressure, and the heat source comes from the first tower top gas phase 112 of the butanone separation tower 11. The first tower top gas phase 112 and the third tower bottom liquid 317 of the ethyl acetate separation tower 31 are heat-exchanged in the second thermally coupled reboiler 32. The third tower bottom liquid 317 is heated and vaporized, and the generated third tower top gas phase 312 is sent to the first thermally coupled reboiler 22 at the bottom of the ethanol separation tower 21 for heat exchange. The obtained second gas-liquid mixture 316 after heat exchange is divided into two parts, one part is the second condensate 319, and the other part is The second uncondensed gas phase 318 is condensed into a third condensed liquid phase 313 through the third collector 33, and enters the third reflux tank 34 together with the second condensate 319, and is forced to reflux and produce through the third reflux pump 36. The third reflux liquid 314 returns to the top of the ethyl acetate separation tower 31, and the third top produced liquid 315 returns to the material inlet of the butanone separation tower 11. The third bottom liquid 317 of the ethyl acetate separation tower 31 is continuously produced with the ethyl acetate product through the third bottom circulation transfer pump 35.

[0022] As a preferred embodiment, the butanone separation tower 11 described in the present invention has an operating pressure of 400-700 kPaG, a theoretical plate number of 40-80, and a reflux ratio of 3-15.

[0023] As a preferred embodiment, the ethanol separation tower 21 described in the present invention has an operating pressure of 30-70 kPaA, a theoretical plate number of 20-60, and a reflux ratio of 1-5.

[0024] As a preferred embodiment, the ethyl acetate separation tower 31 described in the present invention has an operating pressure of normal pressure, a theoretical plate number of 30-80, and a reflux ratio of 2-10.

[0025] Example: The butanone-ethyl acetate-ethanol mixture 111 to be treated has a flow rate of 1000 kg / h, a composition of 31.7% ethyl acetate, 37.5% butanone, and 30.8% ethanol. The operating pressure of the butanone separation tower 11 is 500 kPaG, the number of theoretical plates is 80, the operating reflux ratio is 6, the bottom temperature is 147.2°C, the butanone content produced at the bottom is 99.5%, the production volume is 377 kg / h, the top temperature is 132.5°C, the flow rate of the produced liquid at the top is 3460 kg / h, and the composition is 59.2% ethyl acetate, 10.6% butanone, and 30.2% ethanol. The produced liquid enters the ethanol separation tower 21. The operating pressure of ethanol separation tower 21 is 50 kPaA, the number of theoretical plates is 50, the operating reflux ratio is 3, the tower bottom temperature is 61.5 ° C, the ethanol content of the tower bottom is 99.9%, the production volume is 308 kg / h, the tower top temperature is 53.5 ° C, the flow rate of the tower top produced liquid is 3152 kg / h, and the composition is 65% ethyl acetate, 11.6% butanone, and 23.4% ethanol. The produced liquid enters ethyl acetate separation tower 31. The operating pressure of ethyl acetate separation tower 31 is normal pressure, the number of theoretical plates is 60, the operating reflux ratio is 5, the tower bottom temperature is 76.8 ° C, the ethyl acetate content of the tower bottom is 99.5%, the production volume is 315 kg / h, the tower top temperature is 72 ° C, the flow rate of the tower top produced liquid is 2837 kg / h, and the composition is 61.2% ethyl acetate, 12.9% butanone, and 25.9% ethanol. The produced liquid returns to the butanone separation tower 11.

[0026] like Figure 2As shown, under normal pressure, the components in the ternary mixture of ethanol / ethyl acetate / butanone form three binary minimum azeotropes between each other. Since the ethanol / ethyl acetate azeotropic temperature is lower than the boiling point of ethanol and is also the lowest azeotropic point among the three azeotropes, the two distillation boundary lines formed divide the remaining curve graph into three distillation regions. Among the three azeotropes, the binary azeotropic composition formed by ethanol / ethyl acetate is most sensitive to pressure changes. Therefore, when operating in the distillation region on the upper right side, ethyl acetate can be obtained from the bottom of the tower by a distillation method, and the azeotropes of the remaining two components can be obtained from the top of the tower. When operating in the distillation region on the lower right and lower left sides, the clamping condition is too serious and it is difficult to achieve effective separation.

[0027] like Figure 3 It is shown that when the pressure increases from normal pressure to 600 kPa, the ethanol / ethyl acetate azeotropic composition changes, and the clamping phenomenon of the distillation boundary line is significantly alleviated. Therefore, the distillation area on the lower right side is operated, and butanone can be obtained from the bottom of the tower by distillation, and the azeotropic mixture of the other two components can be obtained from the top of the tower.

[0028] like Figure 4 As shown, when the pressure becomes 50 kPa, the azeotropic composition of ethanol / ethyl acetate changes, and the distillation area on the lower left side is operated. By using the distillation method, ethanol can be obtained from the bottom of the tower, and the azeotropic mixture of the other two components can be obtained from the top of the tower.

[0029] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A separation process for ethyl acetate and butanone, characterized in that: The following steps are involved: The butanone separation tower (11) is operated at a pressurized pressure, the butanone-ethyl acetate-ethanol mixture (111) to be treated enters the middle of the butanone separation tower (11), the first overhead liquid (115) of the butanone separation tower (11) is continuously introduced into the ethanol separation tower (21), and the butanone product is continuously extracted from the bottom of the butanone separation tower (11); the ethanol separation tower (21) is operated at a negative pressure, the second overhead liquid (215) of the ethanol separation tower (21) is continuously introduced into the ethyl acetate separation tower (31), and the ethanol product is continuously extracted from the bottom of the ethanol separation tower (21); the ethyl acetate separation tower (31) is operated at a normal pressure, the third overhead liquid (315) of the ethyl acetate separation tower (31) is returned to the butanone separation tower (11), and the ethyl acetate product is continuously extracted from the bottom of the ethyl acetate separation tower (31).

2. A separation process for ethyl acetate and butanone according to claim 1, characterized in that: The method comprises the following specific steps: the operating pressure of the butanone separation tower (11) is pressurized, the butanone-ethyl acetate-ethanol mixture (111) to be treated enters the middle of the butanone separation tower (11), and under pressurized conditions, steam is used as a heat source to perform indirect heating through a reboiler (12), and the first tower top gas phase (112) generated after heating is used as a heat source to heat the second heat-coupled reboiler (32) of the ethyl acetate separation tower (31), and the gas-liquid mixture (116) after the first heat exchange is divided into two parts, one part is The first condensate (119) and the other part are the first uncondensed gas phase (118). The first uncondensed gas phase (118) is condensed by the first collector (13). The obtained first condensed liquid phase (113) and the first condensate (119) enter the first reflux tank (14) together and are forced to reflux and be produced by the first reflux pump (16). The first reflux liquid (114) returns to the butanone separation tower (11), and the first tower top produced liquid (115) is continuously passed into the ethanol separation tower ( 21), the first bottom liquid (117) of the butanone separation tower (11) is used to continuously extract butanone product through the first bottom circulating material transfer pump (15); the operating pressure of the ethanol separation tower (21) is negative pressure, and the heat source comes from the third top gas phase (312) of the ethyl acetate separation tower (31), which exchanges heat with the second bottom liquid (216) of the ethanol separation tower (21) in the first thermal coupling reboiler (22). After the second bottom liquid (216) is heated and vaporized, its gaseous mixed component is the second top gas phase (2 12) After condensation and cooling in the second collector (23), the second condensed liquid phase (213) enters the second reflux tank (24) and is forced to reflux and extract through the second reflux pump (26). The obtained second reflux liquid (214) is returned to the ethanol separation tower (21). The second tower top extracted liquid (215) is continuously introduced into the ethyl acetate separation tower (31). The second tower bottom liquid (216) of the ethanol separation tower (21) is continuously extracted into the ethanol product through the second tower bottom circulation transfer pump (25);The operating pressure of the ethyl acetate separation tower (31) is atmospheric pressure. The heat source comes from the first tower top gas phase (112) of the butanone separation tower (11). The first tower top gas phase (112) and the third tower bottom liquid (317) of the ethyl acetate separation tower (31) are heat-exchanged in the second thermally coupled reboiler (32). The third tower bottom liquid (317) is heated and vaporized. The generated third tower top gas phase (312) is sent to the first thermally coupled reboiler (22) at the bottom of the ethanol separation tower (21) for heat exchange. After the second heat exchange, the gas-liquid mixture (316) is divided into two parts, one part is the second condensate (319), and the other part is the second condensate (319). The second uncondensed gas phase (318) is condensed into a third condensed liquid phase (313) through a third collector (33), and enters into a third reflux tank (34) together with the second condensate (319), and is forced to reflux and extract through a third reflux pump (36). The third reflux liquid (314) returns to the ethyl acetate separation tower (31), and the third tower top extract liquid (315) returns to the butanone separation tower (11). The third tower bottom liquid (317) of the ethyl acetate separation tower (31) is continuously extracted into an ethyl acetate product through a third tower bottom circulation transfer pump (35). ; 3. The separation process of ethyl acetate and butanone according to claim 1 or 2, characterized in that: The butanone separation tower (11) has an operating pressure of 400-700 kPaG, a theoretical plate number of 40-80, and a reflux ratio of 3-15.

4. The separation process of ethyl acetate and butanone according to claim 3, characterized in that: The operating pressure of the ethanol separation tower (21) is 30-70 kPaA, the number of theoretical plates is 20-60, and the reflux ratio is 1-5.

5. The separation process of ethyl acetate and butanone according to claim 1, characterized in that: The ethyl acetate separation tower (31) has a theoretical plate number of 30-80 and a reflux ratio of 2-10.

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