Separating device for preparing ethanol from dimethyl ether

Abstract

The utility model provides a separation device for preparing ethanol from dimethyl ether, which comprises a pre-separation tower, a degreasing tower I, a degreasing tower II, a methanol tower, an ethanol tower and an ethanol recovery tower which are connected in sequence, a gas phase at the top of the methanol tower provides heat for a pre-separation tower reboiler, a degreasing tower reboiler I, a degreasing tower reboiler II and an ethanol recovery tower reboiler; a gas phase at the top of the ethanol recovery tower provides heat for an ethanol tower reboiler; six main equipment towers including the pre-separation tower, the first degreasing tower, the second degreasing tower, the methanol tower, the ethanol tower and the ethanol recovery tower are adopted, a six-tower thermal coupling process is adopted, a heat exchange network is optimized, and the energy-saving space is enlarged; the device can be used for extracting methanol with the mass fraction of more than 99.9% and ethanol with the mass fraction of more than 97.5%; the efficient utilization of heat in the methanol / ethanol separation process is realized, and the separation energy consumption of a rectification system is reduced; the method is simple in process, economical, practical and high in product yield, and can be used for industrial application of co-production of ethanol and methanol from dimethyl ether.

Description

Technical Field

[0001] This application relates to the technical field of ethanol separation, and specifically relates to a separation device for producing ethanol from dimethyl ether. Background Art

[0002] The method for producing ethanol by the coal chemical route is a method in which coal is used as a raw material to first produce syngas and methanol, and then ethanol is produced by the dimethyl ether method or the acetic acid method; among them, the acetic acid method for producing ethanol is divided into direct hydrogenation of acetic acid to ethanol and hydrogenation of acetate to ethanol. Both methods require the intermediate raw material acetic acid. The economy of ethanol products is greatly affected by acetic acid products, and the production costs are relatively high; for the dimethyl ether method for producing ethanol, there is no acetic acid production link. Methanol is dehydrated to synthesize dimethyl ether. Dimethyl ether and carbon monoxide undergo a dimethyl ether carbonylation reaction to synthesize methyl acetate under the action of a catalyst. Methyl acetate reacts with hydrogen to produce crude ethanol, and the crude ethanol is separated and refined to obtain the product ethanol. This process mainly uses molecular sieve catalysts or copper-based catalysts, without precious metal catalysts, and the production cost is relatively low; only a small amount of acetic acid is generated during the whole reaction process, and the corrosion degree of equipment is very low, so there is no special requirement for equipment materials.

[0003] However, in the process of preparing ethanol by dimethyl ether carbonylation hydrogenation, the energy consumption of the separation section of the reaction products accounts for a relatively large proportion, and a large amount of heat is wasted, resulting in a relatively high steam unit consumption of the whole system. Under the background of the country's increasingly strict requirements for carbon emission indicators, a new technology is needed to recover the heat in the original system to achieve the goal of energy conservation and emission reduction. In view of the material characteristics of this process, researching a new type of highly efficient and energy-saving separation process is of great significance to this ethanol production process.

[0004] The applicant has conducted a search and found the closest prior art as follows:

[0005] A separation method and a separation device for producing ethanol from dimethyl ether with the application number 202210013961.0 disclose a technical solution. The separation device includes a distillation separation system, and the distillation separation system includes a degassing tower, a pre-separation tower, an ethanol tower, and a methanol recovery tower. It can be seen from the attached drawings that this application only utilizes the heat at the top of the pre-separation tower and does not utilize the heat at the tops of other towers, which cannot ensure lower steam energy consumption, and the types and quantities of towers in this application are not the same as the ideas of this application.

[0006] Therefore, a new technical solution is needed to solve the above technical problems. Utility Model Content

[0007] The utility model provides a separation device for producing ethanol from dimethyl ether, which comprises a pre-separation tower, a first de-esterification tower, a second de-esterification tower, a methanol tower, an ethanol tower, and an ethanol recovery tower connected in sequence. Reboilers are respectively arranged at the lower parts of the pre-separation tower, the first de-esterification tower, the second de-esterification tower, the methanol tower, the ethanol tower, and the ethanol recovery tower, namely a pre-separation tower reboiler, a first de-esterification tower reboiler, a second de-esterification tower reboiler, a methanol tower reboiler, an ethanol tower reboiler, and an ethanol recovery tower reboiler. Among them, the gas phase at the top of the methanol tower provides heat for the pre-separation tower reboiler, the first de-esterification tower reboiler, the second de-esterification tower reboiler, and the ethanol recovery tower reboiler; the gas phase at the top of the ethanol recovery tower provides heat for the ethanol tower reboiler.

[0008] As a preferred solution, the top of the methanol tower is connected to the input end of the pre-separation tower reboiler through a first methanol tower top extraction pipeline, and the output end of the pre-separation tower reboiler is connected to a methanol tower reflux device.

[0009] As a preferred solution, the top of the methanol tower is connected to the input end of the first de-esterification tower reboiler through a second methanol tower top extraction pipeline, and the output end of the first de-esterification tower reboiler is connected to a methanol tower reflux device.

[0010] As a preferred solution, the top of the methanol tower is connected to the input end of the second de-esterification tower reboiler through a third methanol tower top extraction pipeline, and the output end of the second de-esterification tower reboiler is connected to a methanol tower reflux device.

[0011] As a preferred solution, the top of the methanol tower is connected to the input end of the ethanol recovery tower reboiler through a fourth methanol tower top extraction pipeline, and the output end of the ethanol recovery tower reboiler is connected to a methanol tower reflux device.

[0012] As a preferred solution, the methanol tower reflux device includes a methanol tower top condenser, which is connected to a methanol tower reflux tank. The bottom of the methanol tower reflux tank is connected to the upper part of the methanol tower through a methanol tower reflux pipeline, and a refined methanol extraction pipeline is arranged at the top of the methanol tower reflux tank.

[0013] As a preferred solution, the top of the ethanol recovery tower is connected to the input end of the ethanol tower reboiler through an ethanol recovery tower top extraction pipeline, and the output end of the ethanol tower reboiler is connected to an ethanol recovery tower reflux device.

[0014] As a preferred solution, the ethanol recovery tower reflux device includes an ethanol recovery tower top condenser connected to the output end of the ethanol tower reboiler. The ethanol recovery tower top condenser is connected to an ethanol recovery tower reflux tank. The bottom of the ethanol recovery tower reflux tank is connected to the upper part of the ethanol recovery tower through an ethanol recovery tower reflux pipeline, and an ethanol extraction pipeline of the ethanol recovery tower is arranged at the top of the ethanol recovery tower reflux tank.

[0015] As a preferred solution, the top of the ethanol tower is connected to an ethanol tower reflux tank through an ethanol tower top draw pipeline. An ethanol tower top condenser is provided on the ethanol tower top draw pipeline. The bottom of the ethanol tower reflux tank is connected to the upper part of the ethanol tower through an ethanol tower reflux pipeline. An ethanol tower ethanol draw pipeline is provided at the top of the ethanol tower reflux tank.

[0016] As a preferred solution, the ethanol draw pipeline of the ethanol recovery tower and the ethanol draw pipeline of the ethanol tower are respectively connected to a mixer, and the output end of the mixer is connected to an ethanol total draw pipeline.

[0017] As a preferred solution, the top of the pre-separation tower is connected to a pre-separation tower top reflux tank through a pre-separation tower top draw pipeline. A pre-separation tower top condenser is provided on the pre-separation tower top draw pipeline. The bottom of the pre-separation tower top reflux tank is connected to the upper part of the pre-separation tower through a pre-separation tower reflux pipeline. A light phase draw pipeline is provided at the top of the pre-separation tower top reflux tank.

[0018] As a preferred solution, the top of the first degreasing tower is connected to a first degreasing tower top reflux tank through a first degreasing tower top draw pipeline. The bottom of the first degreasing tower top reflux tank is connected to the upper part of the first degreasing tower through a first degreasing tower reflux pipeline. A methyl acetate draw pipeline 1 is provided at the top of the first degreasing tower top reflux tank.

[0019] As a preferred solution, the top of the second degreasing tower is connected to a second degreasing tower top reflux tank through a second degreasing tower top draw pipeline. The bottom of the second degreasing tower top reflux tank is connected to the upper part of the second degreasing tower through a second degreasing tower reflux pipeline. A methyl acetate draw pipeline 2 is provided at the top of the second degreasing tower top reflux tank.

[0020] The present application has the following beneficial effects:

[0021] (1) Six main equipment towers, namely a pre-separation tower, a first degreasing tower, a second degreasing tower, a methanol tower, an ethanol tower, and an ethanol recovery tower, are adopted, and a six-tower heat coupling process is used to optimize the heat exchange network and enhance the energy-saving space; the device can produce methanol with a mass fraction of more than 99.9% and ethanol with a mass fraction of more than 97.5%.

[0022] (2) The gas phase at the top of the methanol tower is used to provide heat for the reboilers of the pre-separation tower, the first degreasing tower reboiler, the second degreasing tower reboiler, and the ethanol recovery tower reboiler; the gas phase at the top of the ethanol recovery tower is used to provide heat for the ethanol tower reboiler; through the above heat coupling methods between the towers, efficient heat utilization in the methanol / ethanol separation process is achieved, and the separation energy consumption of the distillation system is reduced.

[0023] (3) Based on the simple, economical and practical process flow and high product yield of the present application, it can be used in the industrial application of producing ethanol from dimethyl ether and co-producing methanol. Brief Description of the Drawings

[0024] Figure 1 is a schematic structural diagram of the present application;

[0025] 1. Pre-separation tower; 2. Feed pipeline; 3. Overhead product pipeline of the pre-separation tower; 4. Overhead reflux drum of the pre-separation tower; 5. Overhead condenser of the pre-separation tower; 6. Reflux pipeline of the pre-separation tower; 7. Light phase product pipeline; 8. Bottoms product pipeline of the pre-separation tower; 9. First de-esterification tower; 10. Overhead product pipeline of the first de-esterification tower; 11. Overhead reflux drum of the first de-esterification tower; 12. Reflux pipeline of the first de-esterification tower; 13. First methyl acetate product pipeline; 14. Bottoms product pipeline of the first de-esterification tower; 15. Second de-esterification tower; 16. Overhead product pipeline of the second de-esterification tower; 17. Overhead reflux drum of the second de-esterification tower; 18. Reflux pipeline of the second de-esterification tower; 19. Second methyl acetate product pipeline; 20. Bottoms product pipeline of the second de-esterification tower; 21. Methanol tower; 22. Bottoms product pipeline of the methanol tower; 23. Ethanol tower; 24. Bottoms product pipeline of the ethanol tower; 25. Ethanol recovery tower; 26. Miscellaneous alcohol product pipeline; 27. Waste liquid product pipeline; 28. Reboiler of the pre-separation tower; 29. First reboiler of the de-esterification tower; 30. Second reboiler of the de-esterification tower; 31. Reboiler of the methanol tower; 32. Reboiler of the ethanol tower; 33. Reboiler of the ethanol recovery tower; 34. First overhead product pipeline of the methanol tower; 35. Output pipeline of the reboiler of the pre-separation tower; 36. Second overhead product pipeline of the methanol tower; 37. Output pipeline of the first reboiler of the de-esterification tower; 38. Third overhead product pipeline of the methanol tower; 39. Output pipeline of the second reboiler of the de-esterification tower; 40. Fourth overhead product pipeline of the methanol tower; 41. Output pipeline of the reboiler of the ethanol recovery tower; 42. Overhead condenser of the methanol tower; 43. Reflux drum of the methanol tower; 44. Reflux pipeline of the methanol tower; 45. Refined methanol product pipeline; 46. Overhead product pipeline of the ethanol recovery tower; 47. Output pipeline of the reboiler of the ethanol tower; 48. Overhead condenser of the ethanol recovery tower; 49. Reflux drum of the ethanol recovery tower; 50. Reflux pipeline of the ethanol recovery tower; 51. Ethanol product pipeline of the ethanol recovery tower; 52. Overhead product pipeline of the ethanol tower; 53. Reflux drum of the ethanol tower; 54. Overhead condenser of the ethanol tower; 55. Reflux pipeline of the ethanol tower; 56. Ethanol product pipeline of the ethanol tower; 57. Mixer; 58. Total ethanol product pipeline; 59. Overhead condenser of the first de-esterification tower; 60. Overhead condenser of the second de-esterification tower. Detailed Description of the Preferred Embodiments

[0026] The following is a detailed description of the specific embodiments of the present invention in conjunction with the accompanying drawings. It should be noted that the specific embodiments described herein are only for the purpose of illustration and explanation of the present invention, and are not intended to limit the present invention.

[0027] Example 1:

[0028] This embodiment provides a separation device for the production of ethanol from dimethyl ether, including a pre-separation tower 1. One side of the pre-fractionation tower 1 is provided with a feed pipeline 2. The reaction product of ethanol production from dimethyl ether enters the pre-separation tower 1 through the feed pipeline 2 for reaction. The top of the pre-separation tower 1 is connected to a pre-separation tower top reflux tank 4 through a pre-separation tower top product extraction pipeline 3. A pre-separation tower top condenser 5 is arranged on the pre-separation tower top product extraction pipeline 3. The bottom of the pre-separation tower top reflux tank 4 is connected to the upper part of the pre-separation tower 1 through a pre-separation tower reflux pipeline 6. The top of the pre-separation tower top reflux tank 4 is provided with a light-phase extraction pipeline 7. The light-phase component is extracted from the top of the pre-separation tower 1. The bottom of the pre-separation tower 1 is connected to a first de-esterification tower 9 through a pre-separation tower bottom product extraction pipeline 8. The top of the first de-esterification tower 9 is connected to a first de-esterification tower top reflux tank 11 through a first de-esterification tower top product extraction pipeline 10. A first de-esterification tower top condenser 59 is arranged on the first de-esterification tower top product extraction pipeline 10. The bottom of the first de-esterification tower top reflux tank 11 is connected to the upper part of the first de-esterification tower 9 through a first de-esterification tower reflux pipeline 12. The top of the first de-esterification tower top reflux tank 11 is provided with a methyl acetate extraction pipeline 13. Part of the methyl acetate at the top of the first de-esterification tower 9 is extracted and part is refluxed to the first de-esterification tower 9. The bottom of the first de-esterification tower 9 is connected to a second de-esterification tower 15 through a first de-esterification tower bottom product extraction pipeline 14. The top of the second de-esterification tower 15 is connected to a second de-esterification tower top reflux tank 17 through a second de-esterification tower top product extraction pipeline 16. A second de-esterification tower top condenser 60 is arranged on the second de-esterification tower top product extraction pipeline 16. The bottom of the second de-esterification tower top reflux tank 17 is connected to the upper part of the second de-esterification tower 15 through a second de-esterification tower reflux pipeline 18. The top of the second de-esterification tower top reflux tank 17 is provided with a methyl acetate extraction pipeline 19. Part of the methyl acetate at the top of the second de-esterification tower 15 is extracted and part is refluxed to the second de-esterification tower 15. The bottom of the second de-esterification tower 15 is connected to a methanol tower 21 through a second de-esterification tower bottom product extraction pipeline 20. The bottom of the methanol tower 21 is connected to an ethanol tower 23 through a methanol tower bottom product extraction pipeline 22. The bottom of the ethanol tower 23 is connected to an ethanol recovery tower 25 through an ethanol tower bottom product extraction pipeline 24. One side of the ethanol recovery tower 25 is provided with a fusel oil extraction pipeline 26. The bottom of the ethanol recovery tower 25 is provided with a waste liquid extraction pipeline 27. The lower parts of the pre-separation tower 1, the first de-esterification tower 9, the second de-esterification tower 15, the methanol tower 21, the ethanol tower 23, and the ethanol recovery tower 25 are respectively provided with a pre-separation tower reboiler 28, a first de-esterification tower reboiler 29, a second de-esterification tower reboiler 30, a methanol tower reboiler 31, an ethanol tower reboiler 32, and an ethanol recovery tower reboiler 33. Among them, the gas phase at the top of the methanol tower 21 provides heat for the pre-separation tower reboiler 28, the first de-esterification tower reboiler 29, the second de-esterification tower reboiler 30, and the ethanol recovery tower reboiler 33. The gas phase at the top of the ethanol recovery tower 25 provides heat for the ethanol tower reboiler 32. The methanol tower reboiler 31 is heated by steam.

[0029] More specifically, the top of the methanol tower 21 is connected to the input end of the pre-separation tower reboiler 28 through the first methanol tower top extraction pipeline 34, and the output end of the pre-separation tower reboiler 28 is connected to the methanol tower reflux device through the pre-separation tower reboiler output pipeline 35; the top of the methanol tower 21 is connected to the input end of the first degreasing tower reboiler 29 through the second methanol tower top extraction pipeline 36, and the output end of the first degreasing tower reboiler 29 is connected to the methanol tower reflux device through the first degreasing tower reboiler output pipeline 37; the top of the methanol tower 21 is connected to the input end of the second degreasing tower reboiler 30 through the third methanol tower top extraction pipeline 38, and the output end of the second degreasing tower reboiler 30 is connected to the methanol tower reflux device through the second degreasing tower reboiler output pipeline 39; the top of the methanol tower 21 is connected to the input end of the ethanol recovery tower reboiler 33 through the fourth methanol tower top extraction pipeline 40, and the output end of the ethanol recovery tower reboiler 33 is connected to the methanol tower reflux device through the ethanol recovery tower reboiler output pipeline 41; wherein, the methanol tower reflux device includes a methanol tower top condenser 42, the methanol tower top condenser 42 is connected to a methanol tower reflux tank 43, the bottom of the methanol tower reflux tank 43 is connected to the upper part of the methanol tower 21 through a methanol tower reflux pipeline 44, and the top of the methanol tower reflux tank 43 is provided with a refined methanol extraction pipeline 45; the refined methanol steam at the top of the methanol tower 21 supplies heat to the pre-separation tower reboiler 28, the first degreasing tower reboiler 29, the second degreasing tower reboiler 30, and the ethanol recovery tower reboiler 33 respectively. The refined methanol after heat exchange can enter the methanol tower top condenser 42 for condensation separately or can be mixed and then enter the methanol tower top condenser 42 for condensation. Specifically, there is no limitation. Technicians can set according to the specific input ports of the methanol tower top condenser 42. For example, Figure 1 As shown, the refined methanol after heat exchange in the pre-separation tower reboiler 28, the first degreasing tower reboiler 29, and the second degreasing tower reboiler 30 is mixed and then enters the methanol tower top condenser 42, and the refined methanol after heat exchange in the ethanol recovery tower reboiler 33 enters the methanol tower top condenser 42 separately; the condensed refined methanol enters the methanol tower reflux tank 43, part of which is refluxed to the methanol tower 21, and part of which is taken out as refined methanol.

[0030] The top of the ethanol recovery column 25 is connected to the input end of the ethanol column reboiler 32 through the ethanol recovery column top draw pipeline 46, and the output end of the ethanol column reboiler 32 is connected to the ethanol recovery column reflux device through the ethanol column reboiler output pipeline 47; the ethanol recovery column reflux device includes an ethanol recovery column top condenser 48 connected to the ethanol column reboiler output pipeline 47, the ethanol recovery column top condenser 48 is connected to the ethanol recovery column reflux drum 49, the bottom of the ethanol recovery column reflux drum 49 is connected to the upper part of the ethanol recovery column 25 through the ethanol recovery column reflux pipeline 50, and the top of the ethanol recovery column reflux drum 49 is provided with an ethanol recovery column ethanol draw pipeline 51; the ethanol vapor at the top of the ethanol recovery column 25 heats the ethanol column reboiler 32, and the heat-exchanged ethanol enters the ethanol recovery column top condenser 48 through the ethanol column reboiler output pipeline 47 for condensation, and the condensed ethanol enters the ethanol recovery column reflux drum 49, and part of the ethanol is refluxed to the ethanol recovery column 25 and part is taken out as ethanol; more preferably, the ethanol drawn from the top of the ethanol column 23 is mixed with the ethanol drawn from the top of the ethanol recovery column 25 and then taken out to ensure that the accuracy of the drawn ethanol reaches more than 99%. Specifically, the top of the ethanol column 23 is connected to the ethanol column reflux drum 53 through the ethanol column top draw pipeline 52, an ethanol column top condenser 54 is provided on the ethanol column top draw pipeline 52, the bottom of the ethanol column reflux drum 53 is connected to the upper part of the ethanol column 23 through the ethanol column reflux pipeline 55, the top of the ethanol column reflux drum 53 is provided with an ethanol column ethanol draw pipeline 56, and the ethanol recovery column ethanol draw pipeline 51 and the ethanol column ethanol draw pipeline 56 are respectively connected to a mixer 57, and the output end of the mixer 57 is connected to an ethanol total draw pipeline 58.

[0031] Embodiment 2:

[0032] This embodiment provides a specific application scenario:

[0033] The top pressure of the pre-separation column 1 is 180 - 220 kPa, the top pressure of the first degreasing column 9 is 100 - 120 kPa, the top pressure of the second degreasing column 15 is 100 - 130 kPa, the top pressure of the methanol column 21 is 300 - 360 kPa, the top pressure of the ethanol column 23 is 20 - 50 kPa, and the top pressure of the ethanol recovery column 25 is 80 - 120 kPa.

[0034] In this application, the specific energy consumption of the dimethyl ether to ethanol distillation process can be reduced from 1.2 t steam / t refined alcohol to 0.50 - 0.60 t steam / t refined alcohol. Compared with the traditional three-column parallel process, it can save more than half of the energy, greatly reduce the operating cost of the enterprise, and improve the competitiveness of the enterprise.

[0035] In summary, due to the adoption of the above technical solutions, this application has the following beneficial effects:

[0036] 1. Six main equipment towers, namely a pre-separation tower, a first de-esterification tower, a second de-esterification tower, a methanol tower, an ethanol tower and an ethanol recovery tower, are adopted. The six-tower heat integration process is used to optimize the heat exchange network and enhance the energy-saving space. This device can produce methanol with a mass fraction of over 99.9% and ethanol with a mass fraction of over 97.5%.

[0037] 2. The top gas phase of the methanol tower is used to provide heat for the reboilers of the pre-separation tower, the first de-esterification tower, the second de-esterification tower and the ethanol recovery tower. The top gas phase of the ethanol recovery tower is used to provide heat for the reboiler of the ethanol tower. Through the above heat integration methods between the towers, the efficient utilization of heat in the methanol / ethanol separation process is achieved, and the separation energy consumption of the distillation system is reduced.

[0038] 3. Based on the simple, economical and practical process flow and high product yield of this application, it can be used in the industrial application of producing ethanol from dimethyl ether and co-producing methanol.

[0039] The devices, connection relationships, etc. not specifically described above all belong to the prior art and will not be specifically elaborated here in the present utility model. They are all conventional technical means and will not be specifically elaborated here. Those skilled in the art can make selections according to specific situations.

[0040] The preferred embodiments of this application have been described in detail above with reference to the accompanying drawings. However, this application is not limited to the specific details in the above embodiments. Within the scope of the technical concept of this application, various simple modifications can be made to the technical solutions of this application, and these simple modifications all fall within the protection scope of this application.

[0041] In addition, it should be noted that the various specific technical features described in the above specific embodiments can be combined in any appropriate manner without conflict. To avoid unnecessary repetition, various possible combination methods of this application will not be described separately.

[0042] Furthermore, any combination can be made between the various different embodiments of this application as long as it does not violate the idea of this application, and it should also be regarded as the content disclosed in this application.

Claims

1. A separation device for the production of ethanol from dimethyl ether, characterized in that, It includes a pre-separation tower (1), a first degreasing tower (9), a second degreasing tower (15), a methanol tower (21), an ethanol tower (23), and an ethanol recovery tower (25) connected in sequence. Reboilers are respectively arranged at the lower parts of the pre-separation tower (1), the first degreasing tower (9), the second degreasing tower (15), the methanol tower (21), the ethanol tower (23), and the ethanol recovery tower (25), namely a pre-separation tower reboiler (28), a first degreasing tower reboiler (29), a second degreasing tower reboiler (30), a methanol tower reboiler (31), an ethanol tower reboiler (32), and an ethanol recovery tower reboiler (33). Among them, the gas phase at the top of the methanol tower (21) provides heat for the pre-separation tower reboiler (28), the first degreasing tower reboiler (29), the second degreasing tower reboiler (30), and the ethanol recovery tower reboiler (33); the gas phase at the top of the ethanol recovery tower (25) provides heat for the ethanol tower reboiler (32).

2. The separation device for dimethyl ether to ethanol according to claim 1, wherein The top of the methanol tower (21) is connected to the input end of the pre-separation tower reboiler (28) through a first methanol tower top extraction pipeline (34), and the output end of the pre-separation tower reboiler (28) is connected to the methanol tower reflux device.

3. The separation device for preparing ethanol from dimethyl ether according to claim 1, characterized in that, The top of the methanol tower (21) is connected to the input end of the first degreasing tower reboiler (29) through a second methanol tower top extraction pipeline (36), and the output end of the first degreasing tower reboiler (29) is connected to the methanol tower reflux device.

4. A separation device for producing ethanol from dimethyl ether according to claim 1, characterized in that, The top of the methanol tower (21) is connected to the input end of the second degreasing tower reboiler (30) through a third methanol tower top extraction pipeline (38), and the output end of the second degreasing tower reboiler (30) is connected to the methanol tower reflux device.

5. A separation device for producing ethanol from dimethyl ether according to claim 1, characterized in that, The top of the methanol tower (21) is connected to the input end of the ethanol recovery tower reboiler (33) through a fourth methanol tower top extraction pipeline (40), and the output end of the ethanol recovery tower reboiler (33) is connected to the methanol tower reflux device.

6. A separation device for producing ethanol from dimethyl ether according to any one of claims 2 - 5, characterized in that, The methanol tower reflux device connection includes a methanol tower top condenser (42), the methanol tower top condenser (42) is connected to a methanol tower reflux tank (43), the bottom of the methanol tower reflux tank (43) is connected to the upper part of the methanol tower (21) through a methanol tower reflux pipeline (44), and a refined methanol extraction pipeline (45) is arranged at the top of the methanol tower reflux tank (43).

7. A separation device for producing ethanol from dimethyl ether according to claim 1, characterized in that, The top of the ethanol recovery tower (25) is connected to the input end of the ethanol tower reboiler (32) through an ethanol recovery tower top extraction pipeline (46), and the output end of the ethanol tower reboiler (32) is connected to the ethanol recovery tower reflux device.

8. A separation device for producing ethanol from dimethyl ether according to claim 7, characterized in that, The ethanol recovery tower reflux device includes an ethanol recovery tower top condenser (48) connected to the output end of the ethanol tower reboiler (32), the ethanol recovery tower top condenser (48) is connected to an ethanol recovery tower reflux tank (49), the bottom of the ethanol recovery tower reflux tank (49) is connected to the upper part of the ethanol recovery tower (25) through an ethanol recovery tower reflux pipeline (50), and an ethanol extraction pipeline of the ethanol recovery tower (51) is arranged at the top of the ethanol recovery tower reflux tank (49).

9. A separation device for the production of ethanol from dimethyl ether according to claim 8, characterized in that, The top of the ethanol column (23) is connected to the ethanol column reflux drum (53) through the ethanol column top draw pipeline (52). An ethanol column top condenser (54) is provided on the ethanol column top draw pipeline (52). The bottom of the ethanol column reflux drum (53) is connected to the upper part of the ethanol column (23) through the ethanol column reflux pipeline (55). An ethanol column ethanol draw pipeline (56) is provided at the top of the ethanol column reflux drum (53).

10. A separation device for producing ethanol from dimethyl ether according to claim 9, characterized in that, The ethanol column ethanol draw pipeline (51) and the ethanol column ethanol draw pipeline (56) are respectively connected to a mixer (57). The output end of the mixer (57) is connected to an ethanol total draw pipeline (58).

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